CN203402928U - Resourceful treatment process system for ammonia-containing waste gas/steam in production process of ammonium paratungstate - Google Patents
Resourceful treatment process system for ammonia-containing waste gas/steam in production process of ammonium paratungstate Download PDFInfo
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- CN203402928U CN203402928U CN201320496791.2U CN201320496791U CN203402928U CN 203402928 U CN203402928 U CN 203402928U CN 201320496791 U CN201320496791 U CN 201320496791U CN 203402928 U CN203402928 U CN 203402928U
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Abstract
The utility model discloses a resourceful treatment process system for ammonia-containing waste gas/steam in the production process of ammonium paratungstate. The system comprises a gas/steam water separator (1), an absorption tower (2), a weak aqua ammonia regulating reservoir (4) and a concentration tower (7). A gas outlet of the gas/steam water separator (1) is connected with the absorption tower (2); a liquid outlet of the gas/steam water separator (1) and a liquid outlet of the absorption tower (2) are connected with the weak aqua ammonia regulating reservoir (4), and the weak aqua ammonia regulating reservoir (4) is connected with the concentration tower (7). The resourceful treatment process system for the ammonia-containing waste gas/steam in the production process of the ammonium paratungstate can achieve recovery of ammonia in the waste gas/steam as high-concentration and high-quality ammonia water and also can achieve cyclic utilization of water in the treatment process system.
Description
Technical field
The utility model relates to the resource type treating process system of the ammonia-contaminated gas/vapour producing in a kind of ammonium paratungstate (APT) production process, belong to metallurgy industry tungsten smelting technology, be also applicable to the recycling treatment of the ammonia-contaminated gas that produces in other Metal smelting processes of metallurgy industry.
Background technology
Ammonia-contaminated gas/vapour in ammonium paratungstate (APT) production process, the source of ammonia-contaminated gas be mainly that ammonium tungstate continuous evaporative crystallization produces containing ammonia steam (consecutive evaporation, double evaporation-cooling), the NH of ammonium paratungstate calcining tail gas after pickling
3gas.Traditional art breading ammonia-contaminated gas has absorption process, extraction method of enrichment, reactive absorption method etc., and each method also has applicable condition.
Absorption process is the most traditional method, and relatively early, comparison in equipment is simple in application, operates more conveniently, and assimilation effect can reach 80%.But owing to limited by processing condition, absorption liquid can not reuse, must after processing, sewage work could discharge.So water loss is larger, running cost is higher, and does not meet resource rational utilization recovery principle.
Extraction absorption process is applicable to the gas that composition is relatively single, and gas is higher containing ammonia concentration ratio.But extraction liquid cost compare is high, after extraction, separating difficulty is larger, and separating device needs many, so this method reclaims ammonia now, is of little use.
The gas that the utilization of reactive absorption method contains sulfurous gas or nitrogen peroxide, first wet and close with ammonia-contaminated gas, again by spray absorber, the stability that generates ammonium sulfide by ammonia powerful solvability and reaction in water, effectively removes the gases such as the ammonia of gas and sulfur oxide.In the water using, need to add liming, reaction generates calcium sulfate precipitation, need to could reuse circulation fluid after calcium sulfate precipitation separation, and needs to add liming in the circulation fluid of recycling again.
Smelt tungsten and produce the traditional treatment process of ammonia-contaminated gas, generally take recovery, the neutralization reaction of two-stage.Primary amine recovery process, after one-level recovery process, neutralizes in secondary and to remaining ammonia in gas again, and neutralization reaction can reclaim a part of ammonium salt.But after two stages for the treatment of, the residual content of ammonia can meet emission standard requirement.Generally there is following problem in the waste gas pollution control and treatment producing at tungsten smelting process at present:
1, traditional technology generally all can only reclaim a part of ammonia, or by neutralization reaction, generates ammonium salt, but no matter is to reclaim, or the ammonium salt generating by neutralization, and the resource recovery of ammonia is not high.
2,, during traditional technology is processed, because the rate of recovery of ammonia is not high, and recovery ammonia can not be directly used in production.Remaining ammonia can only be processed through absorption or chemical reaction, and this mode just realizes ammonia and shifts, and can not realize resource utilization and recycling, and ammonia content directly discharges after reaching emission standard.
3, the absorption of ammonia-contaminated gas/vapour in traditional technology system, owing to being subject to the restriction of condition equipment, the ammonia of recovery can not be produced by direct reuse, must process through sewage work, and in processing engineering, processing cost increases, and whole process system water loss is also very large.
4, traditional technology absorbs the ammonia in ammonia-contaminated gas, and general the processing for high density ammonia-contaminated gas, if the ammonia concentration ratio in waste gas is lower, can strengthen ammoniacal liquor recovery difficult, reduces economy.
Utility model content
In order to overcome above-mentioned the deficiencies in the prior art, the utility model provides ammonia-contaminated gas/vapour recycling treatment process system in a kind of ammonium paratungstate (APT) production process, solved the recycling treatment problem that produces ammonia-contaminated gas/vapour in tungsten smelting process, and the high strength ammonia reclaiming can direct reuse in production technique system.In this treatment process system, the water of cooling ammonia steam after heat exchange, is back to absorption tower again, realizes the recycle of water in system, reduces running cost.
In order to achieve the above object, the utility model has adopted following technical scheme:
A recycling treatment process system for the ammonia-contaminated gas/vapour producing in process, described system comprises gas/steam separator, absorption tower, weak ammonia equalizing tank and concentration tower;
The pneumatic outlet of described gas/steam separator is connected with absorption tower;
The liquid exit on described gas/steam separator and absorption tower is all connected with weak ammonia equalizing tank;
Described weak ammonia equalizing tank is connected with concentration tower.
"/" described in the present invention in " ammonia-contaminated gas/vapour " represent " with " or "or".
"/" in " gas/steam separator " of the present invention represent " with " or "or".
In the present invention, ammonia-contaminated gas/vapour that the calcining of ammonium paratungstate (APT) production process, evaporation produce, passes through gas/steam separator together, and condensation is absorbed as the ammoniacal liquor (mass concentration is no more than 15% condensation ammoniacal liquor) of lower concentration and is transported to weak ammonia equalizing tank.
Preferably, described gas/steam separator is provided with ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization exhaust gas entrance, and described gas/steam separator also comprises an Ammonia vapour Condenser.
Preferably, described gas/steam separator is also provided with ammonium tungstate mother liquor double evaporation-cooling crystallization exhaust gas entrance.
Described ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization waste gas and ammonium tungstate mother liquor double evaporation-cooling crystallization exhaust gas are the ammonia-contaminated gas/vapour of the calcining of APT production process, evaporation generation.
While only containing ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization waste gas in ammonia-contaminated gas/vapour that described APT production process calcining, evaporation produce, described waste gas enters gas/steam separator through ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization exhaust gas entrance, first through Ammonia vapour Condenser, then carry out gas/carbonated drink separated, obtain the weak ammonia (mass concentration is no more than 15% condensation ammoniacal liquor) of lower concentration.
In ammonia-contaminated gas/vapour that described APT production process calcining, evaporation produce, ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization waste gas had both been contained, while also containing ammonium tungstate mother liquor double evaporation-cooling crystallization exhaust gas, it enters gas/steam separator through entrance separately respectively.Wherein, ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization waste gas, first through Ammonia vapour Condenser, then carry out the separation of gas/carbonated drink, obtain the weak ammonia of lower concentration.Ammonium tungstate mother liquor double evaporation-cooling crystallization exhaust gas is directly carried out the separation of gas/carbonated drink, obtains the weak ammonia of lower concentration.Above-mentioned two strands of weak ammonias are transported to weak ammonia equalizing tank.The remaining pneumatic outlet from gas/steam separator is discharged nonabsorbable waste gas, gas after absorption still has a certain amount of ammonia, now directly use again condensation, assimilation effect to ammonia is bad, and high cost, so remaining from gas/steam separator pneumatic outlet nonabsorbable ammonia-contaminated gas/vapour of discharging enter absorption tower.From the pneumatic outlet expellant gas of gas/steam separator, entering absorption tower absorbs, through absorption tower, absorb the weak ammonia forming and enter weak ammonia equalizing tank, several strands of weak ammonias carry out intimate mixing in weak ammonia equalizing tank, through weak ammonia lift pump, enter concentration tower, carry out stripping, obtain high density ammoniacal liquor.Wherein, the ammoniacal liquor in weak ammonia equalizing tank is that mass concentration is no more than 15% ammoniacal liquor.
Preferably, described concentration tower tower top is provided with pneumatic outlet and backflow ammonia inlet, and tower middle part is provided with weak ammonia entrance, is provided with steam-in and water outlet at the bottom of tower.
Preferably, described weak ammonia equalizing tank is connected with concentration tower by weak ammonia entrance, makes the ammoniacal liquor in weak ammonia equalizing tank by weak ammonia entrance, enter concentration tower under the effect of pump.
Preferably, between described weak ammonia equalizing tank and concentration tower, be provided with feed preheater, at the bottom of the tower of described feed preheater and concentration tower, water outlet is connected.Weak ammonia in weak ammonia equalizing tank is undertaken entering concentration tower after heat exchange by the pressurize tower reactor high-temperature water of incoming stock preheater and concentration tower of pump.To entering the weak ammonia raw material of concentration tower, carry out preheating lifting temperature, saved steam consumption in process system, improved heat utilization efficiency, reduced overall energy consumption.
Preferably, after described feed preheater, be provided with cooling heat exchanger, it is connected with absorption tower, so that the water cooling of discharging from water outlet at the bottom of the tower of concentration tower enters absorption tower and recycles.In concentration tower through after vapor liquid equilibrium repeatedly, along with ammonia constantly volatilizees, ammonia concentration in concentration tower liquid is more come also low, to at the bottom of tower time, ammonia concentration in water has been reduced to the requirement on absorption tower, and the first incoming stock preheater of liquid, enters cooling heat exchanger afterwards, after two-stage heat exchange cooling, reuse, to absorption tower, has realized the internal recycling utilization of water again.
Preferably, described concentration tower overhead gas outlet connects the entrance of overhead condenser, and the outlet of described overhead condenser is connected with backflow ammonia inlet, and described overhead condenser is also connected with tank used for storing ammonia.In concentration tower, entered after gas-liquid phase equilibrium repeatedly, ammonia concentration in gas phase reaches the concentration requirement of design, then entering overhead condenser liquefies completely, an ammoniacal liquor part after liquefaction is transported to tank used for storing ammonia (ammoniacal liquor mass concentration >=15% that recovery obtains) as product, a part is back in concentration tower by backflow ammonia inlet, then participates in the gas-liquid phase equilibrium in tower.
Preferably, the thermal source needing in described concentration tower, its thermal source source, can be direct Boiler Steam, also can utilize the waste water, the waste gas/vapour waste heat that in production process, produce.
Preferably, the progression on described absorption tower can be n level, n=1～10.The tower top on described absorption tower is connected with blower fan, and when absorption tower is while being multistage (when n is greater than 1), blower fan is connected with last step absorption tower, makes the tower top residual gas in absorption tower be delivered to and be built up the chimney that meets discharging standards height by blower fan.
Preferably, described Ammonia vapour Condenser comprises one or more vertical or horizontal condenser combinations, and vertical or horizontal condenser is shell, sleeve pipe, board-like or spiral plate type.
Preferably, the internal structure on described absorption tower can be hollow-spraying-tower formula, material filling type, shell and tube, board-like, rapid ball formula, and absorption tower internal structure comprises these forms but is not limited to these these.
The working process of the utility model system is roughly as follows:
Ammonia-contaminated gas/vapour in ammonium paratungstate (APT) production process, passes through gas/steam separator together, and water is wherein separated, and obtains weak ammonia simultaneously, and weak ammonia enters weak ammonia equalizing tank.From the pneumatic outlet expellant gas of gas/steam separator, enter absorption tower and absorb, absorb the weak ammonia forming enter weak ammonia equalizing tank through absorption tower, tower top residual gas is delivered to and is built up the chimney that meets discharging standards height by blower fan.Several strands of weak ammonias carry out average mixing in weak ammonia equalizing tank, and ammoniacal liquor promotes through pump, first passes through feed preheater, carries out heat exchange with concentration tower tower reactor high-temperature water, enters after heat exchange, enters concentration tower.Because the volatility of ammonia is greater than water, under the effect of steam, the ammonia in weak ammonia proceeds to gas phase state.In concentration tower, after gas-liquid phase equilibrium repeatedly, ammonia concentration in gas phase reaches the concentration requirement of design, then entering overhead condenser liquefies completely, an ammoniacal liquor part after liquefaction is transported to tank used for storing ammonia as product, a part is back in ammonia concentration tower, then participates in the gas-liquid phase equilibrium in tower.Liquid in concentration tower, continuous evaporation along with ammonia, ammonia in liquid lowers gradually, and at the bottom of tower time, the ammonia in liquid has been reduced to the service requirements on absorption tower, first the liquid of at this moment discharging from water outlet at the bottom of tower pass through feed preheater, carry out heat exchange with the weak ammonia entering before tower, feed preheater water outlet, to cooling heat exchanger, is back to use in absorption tower afterwards again, not only realize the recycle of technique internal water, also the raw material entering before tower is carried out to preheating simultaneously.
Compared with prior art, the utlity model has following beneficial effect:
The beneficial effects of the utility model are: compared with prior art, solved in tungsten smelting process, produce containing ammonia vapor recovery ammoniacal liquor product concentration is little, purity is a low difficult problem, also solve in waste gas/vapour low concentration ammonia recovery difficult large simultaneously, rely on to shift just can make a difficult problem for waste gas qualified discharge, whole process system in the process of processing waste gas, realize sewage zero release.In whole treatment process process, water is recycle not only, carries out preheating lifting temperature to entering tower raw material simultaneously, has saved steam consumption in process system.In whole treatment process system, do not have the medicaments such as other catalyzer, neutralizing agent, coagulation to add, realize zero of off gas treatment reagent cost and add.
Accompanying drawing explanation
Below in conjunction with accompanying drawing and by embodiment, further illustrate the technical solution of the utility model.
Fig. 1: the ammonia-contaminated gas/vapour recycling treatment process system schematic producing in a kind of ammonium paratungstate (APT) production process.
In the utility model Figure of description, mark is as follows:
1-gas/steam separator 2-absorption tower 3-blower fan 4-weak ammonia equalizing tank 5-feed preheater
Ammonia-contaminated gas/vapour in 6-cooling heat exchanger 7-concentration tower 8-overhead condenser 9-APT production process.
Embodiment
For the utility model is described better, be convenient to understand the technical solution of the utility model, typical but non-limiting embodiment of the present utility model is as follows:
Embodiment 1
A recycling treatment process system for the ammonia-contaminated gas/vapour producing in process, described system comprises gas/steam separator 1, absorption tower 2, weak ammonia equalizing tank 4, concentration tower 7.Described gas/steam separator 1 pneumatic outlet is connected with absorption tower 2.The liquid exit on gas/steam separator 1 and absorption tower 2 is all connected with weak ammonia equalizing tank 4.Described concentration tower 7 tower tops are provided with pneumatic outlet and backflow ammonia inlet, and tower middle part is provided with weak ammonia entrance, is provided with steam-in and water outlet at the bottom of tower.Described weak ammonia equalizing tank 4 is connected with concentration tower 7 by weak ammonia entrance, between weak ammonia equalizing tank 4 and concentration tower 7, is provided with feed preheater 5, and at the bottom of the tower of feed preheater 5 and concentration tower 7, water outlet is connected.After described feed preheater 5, be provided with cooling heat exchanger 6, it is connected with absorption tower 2, so that the water cooling of discharging from water outlet at the bottom of the tower of concentration tower 7 enters absorption tower 2 and recycles.The pneumatic outlet of concentration tower 7 connects the entrance of overhead condenser 8, and its outlet is connected with backflow ammonia inlet, and described overhead condenser 8 is also connected with tank used for storing ammonia.The tower top on absorption tower 2 is connected with blower fan 3.
The working process of the utility model system is roughly as follows:
Ammonia-contaminated gas/vapour that the calcining of APT production process, evaporation produce, passes through gas/steam separator 1 together, and condensation is absorbed as the ammoniacal liquor (mass concentration is no more than 15% condensation ammoniacal liquor) of lower concentration and is transported to weak ammonia equalizing tank 4.
From the pneumatic outlet expellant gas of gas/steam separator 1, enter absorption tower 2 and absorb, through absorption tower, 2 absorb the weak ammonias that form and enter weak ammonia equalizing tank 4, and tower top residual gas is delivered to and is built up the chimney that meets discharging standards height by blower fan 3.Several strands of weak ammonias carry out intimate mixing in weak ammonia equalizing tank 4, and ammoniacal liquor promotes through pump, first passes through feed preheater 5, carries out heat exchange with concentration tower 7 tower reactor high-temperature water, enters after heat exchange, enters concentration tower 7.Because the volatility of ammonia is greater than water, under the effect of steam, the ammonia in weak ammonia proceeds to gas phase state.In concentration tower 7, entered after gas-liquid phase equilibrium repeatedly, ammonia concentration in gas phase reaches the concentration requirement of design, then entering overhead condenser 8 liquefies completely, an ammoniacal liquor part after liquefaction is transported to tank used for storing ammonia as product, a part is back in concentration tower 7, then participates in the gas-liquid phase equilibrium in tower.Liquid in concentration tower 7, continuous evaporation along with ammonia, ammonia in liquid lowers gradually, and at the bottom of tower time, the ammonia in liquid has eased down to the service requirements on absorption tower 2, first the liquid of at this moment discharging from water outlet at the bottom of tower pass through feed preheater 5, carry out heat exchange with the weak ammonia entering before concentration tower 7, feed preheater 5 water outlets, to cooling heat exchanger 6, are back to use in absorption tower 2 afterwards again, not only realize the recycle of technique internal water, also the raw material entering before tower is carried out to preheating simultaneously.
In the recycling treatment process system of ammonia-contaminated gas/vapour of producing, described system comprises gas/steam separator 1, absorption tower 2, weak ammonia equalizing tank 4, concentration tower 7.Described gas/steam separator 1 is provided with the entrance of ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization waste gas, and its pneumatic outlet is connected with absorption tower 2.The liquid exit on gas/steam separator 1 and absorption tower 2 is all connected with weak ammonia equalizing tank 4.Described gas/steam separator 1 also comprises an Ammonia vapour Condenser.Described concentration tower 7 tower tops are provided with pneumatic outlet and backflow ammonia inlet, and tower middle part is provided with weak ammonia entrance, is provided with steam-in and water outlet at the bottom of tower.Described weak ammonia equalizing tank 4 is connected with concentration tower 7 by weak ammonia entrance, between weak ammonia equalizing tank 4 and concentration tower 7, is provided with feed preheater 5, and at the bottom of the tower of feed preheater 5 and concentration tower 7, water outlet is connected.After described feed preheater 5, be provided with cooling heat exchanger 6, it is connected with absorption tower 2, so that the water cooling of discharging from water outlet at the bottom of the tower of concentration tower 7 enters absorption tower 2 and recycles.The pneumatic outlet of concentration tower 7 connects the entrance of overhead condenser 8, and its outlet is connected with backflow ammonia inlet, and described overhead condenser 8 is also connected with tank used for storing ammonia.The tower top on absorption tower 2 is connected with blower fan 3.
The working process of the utility model system is roughly as follows:
Ammonia-contaminated gas/vapour that the calcining of APT production process, evaporation produce, passes through gas/steam separator 1 together, and condensation is absorbed as the ammoniacal liquor (mass concentration is no more than 15% condensation ammoniacal liquor) of lower concentration and is transported to weak ammonia equalizing tank 4.
The technical process of described gas/steam separator is as follows:
In ammonia-contaminated gas/vapour that described APT production process calcining, evaporation produce, only contain ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization waste gas, described waste gas enters gas/steam separator 1 through ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization exhaust gas entrance, first through Ammonia vapour Condenser, then carry out gas/carbonated drink separated, obtain the weak ammonia (mass concentration is no more than 15% condensation ammoniacal liquor) of lower concentration.
From the pneumatic outlet expellant gas of gas/steam separator 1, enter absorption tower 2 and absorb, through absorption tower, 2 absorb the weak ammonias that form and enter weak ammonia equalizing tank 4, and tower top residual gas is delivered to and is built up the chimney that meets discharging standards height by blower fan 3.Several strands of weak ammonias carry out intimate mixing in weak ammonia equalizing tank 4, and ammoniacal liquor promotes through pump, first passes through feed preheater 5, carries out heat exchange with concentration tower 7 tower reactor high-temperature water, enters after heat exchange, enters concentration tower 7.Because the volatility of ammonia is greater than water, under the effect of steam, the ammonia in weak ammonia proceeds to gas phase state.In concentration tower 7, entered after gas-liquid phase equilibrium repeatedly, ammonia concentration in gas phase reaches the concentration requirement of design, then entering overhead condenser 8 liquefies completely, an ammoniacal liquor part after liquefaction is transported to tank used for storing ammonia as product, a part is back in concentration tower 7, then participates in the gas-liquid phase equilibrium in tower.Liquid in concentration tower 7, continuous evaporation along with ammonia, ammonia in liquid lowers gradually, and at the bottom of tower time, the ammonia in liquid has eased down to the service requirements on absorption tower 2, first the liquid of at this moment discharging from water outlet at the bottom of tower pass through feed preheater 5, carry out heat exchange with the weak ammonia entering before concentration tower 7, feed preheater 5 water outlets, to cooling heat exchanger 6, are back to use in absorption tower 2 afterwards again, not only realize the recycle of technique internal water, also the raw material entering before tower is carried out to preheating simultaneously.
In the recycling treatment process system of ammonia-contaminated gas/vapour of producing, described system comprises gas/steam separator 1, absorption tower 2, weak ammonia equalizing tank 4, concentration tower 7.Described gas/steam separator 1 is provided with the entrance of ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization waste gas, and described gas/steam separator 1 is also provided with ammonium tungstate mother liquor double evaporation-cooling crystallization exhaust gas entrance, and its pneumatic outlet is connected with absorption tower 2.The liquid exit on gas/steam separator 1 and absorption tower 2 is all connected with weak ammonia equalizing tank 4.Described gas/steam separator 1 also comprises an Ammonia vapour Condenser.Described concentration tower 7 tower tops are provided with pneumatic outlet and backflow ammonia inlet, and tower middle part is provided with weak ammonia entrance, is provided with steam-in and water outlet at the bottom of tower.Described weak ammonia equalizing tank 4 is connected with concentration tower 7 by weak ammonia entrance, between weak ammonia equalizing tank 4 and concentration tower 7, is provided with feed preheater 5, and at the bottom of the tower of feed preheater 5 and concentration tower 7, water outlet is connected.After described feed preheater 5, be provided with cooling heat exchanger 6, it is connected with absorption tower 2, so that the water cooling of discharging from water outlet at the bottom of the tower of concentration tower 7 enters absorption tower 2 and recycles.The pneumatic outlet of concentration tower 7 connects the entrance of overhead condenser 8, and its outlet is connected with backflow ammonia inlet, and described overhead condenser 8 is also connected with tank used for storing ammonia.The tower top on absorption tower 2 is connected with blower fan 3.
The working process of the utility model system is roughly as follows:
Ammonia-contaminated gas/vapour that the calcining of APT production process, evaporation produce, passes through gas/steam separator 1 together, and condensation is absorbed as the ammoniacal liquor (mass concentration is no more than 15% condensation ammoniacal liquor) of lower concentration and is transported to weak ammonia equalizing tank 4.
The technical process of described gas/steam separator is as follows:
In ammonia-contaminated gas/vapour that described APT production process calcining, evaporation produce, ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization waste gas had both been contained, also contain ammonium tungstate mother liquor double evaporation-cooling crystallization exhaust gas, it enters gas/steam separator 1 through entrance separately respectively.Wherein, ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization waste gas, first through Ammonia vapour Condenser, then carry out the separation of gas/carbonated drink, obtain the weak ammonia of lower concentration.Ammonium tungstate mother liquor double evaporation-cooling crystallization exhaust gas is directly carried out the separation of gas/carbonated drink, obtains the weak ammonia of lower concentration.
From the pneumatic outlet expellant gas of gas/steam separator 1, enter absorption tower 2 and absorb, through absorption tower, 2 absorb the weak ammonias that form and enter weak ammonia equalizing tank 4, and tower top residual gas is delivered to and is built up the chimney that meets discharging standards height by blower fan 3.Several strands of weak ammonias carry out intimate mixing in weak ammonia equalizing tank 4, and ammoniacal liquor promotes through pump, first passes through feed preheater 5, carries out heat exchange with concentration tower 7 tower reactor high-temperature water, enters after heat exchange, enters concentration tower 7.Because the volatility of ammonia is greater than water, under the effect of steam, the ammonia in weak ammonia proceeds to gas phase state.In concentration tower 7, entered after gas-liquid phase equilibrium repeatedly, ammonia concentration in gas phase reaches the concentration requirement of design, then entering overhead condenser 8 liquefies completely, an ammoniacal liquor part after liquefaction is transported to tank used for storing ammonia as product, a part is back in concentration tower 7, then participates in the gas-liquid phase equilibrium in tower.Liquid in concentration tower 7, continuous evaporation along with ammonia, ammonia in liquid lowers gradually, and at the bottom of tower time, the ammonia in liquid has eased down to the service requirements on absorption tower 2, first the liquid of at this moment discharging from water outlet at the bottom of tower pass through feed preheater 5, carry out heat exchange with the weak ammonia entering before concentration tower 7, feed preheater 5 water outlets, to cooling heat exchanger 6, are back to use in absorption tower 2 afterwards again, not only realize the recycle of technique internal water, also the raw material entering before tower is carried out to preheating simultaneously.
Applicant's statement, the utility model illustrates detailed structure feature of the present utility model and treatment process by above-described embodiment, but the utility model is not limited to above-mentioned detailed structure feature and treatment process, do not mean that the utility model must rely on above-mentioned detailed structure feature and treatment process could be implemented.Person of ordinary skill in the field should understand; to any improvement of the present utility model; to the selection of the interpolation of the equivalence replacement of the selected parts of the utility model product and accessory, concrete mode etc., within all dropping on protection domain of the present utility model and open scope.
Claims (10)
1. a recycling treatment process system for ammonia-contaminated gas/vapour in ammonium paratungstate production process, is characterized in that, described system comprises gas/steam separator (1), absorption tower (2), weak ammonia equalizing tank (4) and concentration tower (7);
The pneumatic outlet of described gas/steam separator (1) is connected with absorption tower (2);
The liquid exit of described gas/steam separator (1) and absorption tower (2) is all connected with weak ammonia equalizing tank (4);
Described weak ammonia equalizing tank (4) is connected with concentration tower (7).
2. the system as claimed in claim 1, it is characterized in that, described gas/steam separator (1) is provided with ammonium paratungstate calcining waste gas and ammonium tungstate continuous evaporative crystallization exhaust gas entrance, described gas/steam separator (1) also comprises an Ammonia vapour Condenser, and described gas/steam separator (1) is also provided with ammonium tungstate mother liquor double evaporation-cooling crystallization exhaust gas entrance.
3. the system as claimed in claim 1, is characterized in that, described concentration tower (7) tower top is provided with pneumatic outlet and backflow ammonia inlet, and tower middle part is provided with weak ammonia entrance, is provided with steam-in and water outlet at the bottom of tower.
4. system as claimed in claim 3, is characterized in that, described weak ammonia equalizing tank (4) is connected with concentration tower (7) by weak ammonia entrance, and is provided with feed preheater (5) between described weak ammonia equalizing tank (4) and concentration tower (7).
5. system as claimed in claim 4, is characterized in that, at the bottom of the tower of described feed preheater (5) and concentration tower (7), water outlet is connected.
6. system as claimed in claim 5, is characterized in that, is provided with cooling heat exchanger (6) after described feed preheater (5), and it is connected with absorption tower (2), so that the water cooling from discharging at the bottom of the tower of concentration tower (7) enters absorption tower (2) and recycles.
7. system as claimed in claim 3, it is characterized in that, the outlet of described concentration tower (7) overhead gas connects the entrance of overhead condenser (8), and the outlet of described overhead condenser (8) is connected with backflow ammonia inlet, and described overhead condenser (8) is also connected with tank used for storing ammonia.
8. the system as claimed in claim 1, is characterized in that, the progression of described absorption tower (2) is n level, n=1～10.
9. the system as claimed in claim 1, is characterized in that, the tower top of described absorption tower (2) is connected with blower fan (3), and when described absorption tower (2) are multistage, blower fan (3) is connected with last step absorption tower.
10. system as claimed in claim 2, is characterized in that, described Ammonia vapour Condenser comprises one or more vertical or horizontal condenser combinations, and vertical or horizontal condenser is shell, sleeve pipe, board-like or spiral plate type.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104310426A (en) * | 2014-10-09 | 2015-01-28 | 中国有色集团（广西）平桂飞碟股份有限公司 | Process of recovering ammonia from ammonia-nitrogen wastewater and exhaust gas of tungsten metallurgy |
| CN106823692A (en) * | 2017-03-22 | 2017-06-13 | 天华化工机械及自动化研究设计院有限公司 | A kind of ammonia-contaminated gas zero-emission and ammonia reclaiming process |
| CN108722122A (en) * | 2018-05-29 | 2018-11-02 | 王志强 | Industrial tungsten fusion process tail gas recycle utilizes processing method and equipment |
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2013
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104310426A (en) * | 2014-10-09 | 2015-01-28 | 中国有色集团（广西）平桂飞碟股份有限公司 | Process of recovering ammonia from ammonia-nitrogen wastewater and exhaust gas of tungsten metallurgy |
| CN104310426B (en) * | 2014-10-09 | 2016-06-08 | 中国有色集团（广西）平桂飞碟股份有限公司 | A kind of technique reclaiming ammonia from Tungsten smelting ammonia nitrogen waste water waste gas |
| CN106823692A (en) * | 2017-03-22 | 2017-06-13 | 天华化工机械及自动化研究设计院有限公司 | A kind of ammonia-contaminated gas zero-emission and ammonia reclaiming process |
| CN108722122A (en) * | 2018-05-29 | 2018-11-02 | 王志强 | Industrial tungsten fusion process tail gas recycle utilizes processing method and equipment |
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