CN102358625B - Garbage-percolate evaporating and concentrating processing method capable of recycling ammonia and device thereof - Google Patents
Garbage-percolate evaporating and concentrating processing method capable of recycling ammonia and device thereof Download PDFInfo
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Abstract
The invention discloses a garbage-percolate evaporating and concentrating processing method capable of recycling ammonia, which comprises the following steps that: (1) garbage percolate is sent into a heating chamber of an evaporator to be evaporated and concentrated to form secondary steam and dischargeable concentrated liquid; (2) ammonia recycling treatment is undertaken for the secondary steam produced in the step (1); and (3) the secondary steam after the ammonia recycling treatment is sent into a heating tube in the evaporator in the step (1) through a pipeline to be used as a heat source for evaporating the garbage percolate. The invention also discloses a garbage-percolate evaporating and concentrating processing device for realizing the above method. Due to the method, the garbage percolate or high-ammonia high-organism high-salt waste water is evaporated, so the ammonia and volatile organisms in the waste water can be evaporated to form secondary steam with the vapor, the ammonia is recycled and the organisms are removed during the flowing process of the secondary steam, and further the method also has the characteristics of thorough absorption and easiness in implementation under the situation that the processed distilled water conforms to relevant emission standards.
Description
Technical field
The present invention relates to a kind of percolate evaporation concentration treatment process and equipment thereof, relate in particular to and a kind ofly can carry out percolate that ammonia reclaims or evaporation concentration treatment process and the equipment thereof of high-concentration waste water.
Background technology
Along with the increase of China's urban population, the expansion of city size and the raising of resident living level, the output of China's domestic waste also sharply increases.The main processing mode of municipal wastes has garbage loading embeading, burning, compost etc. at present.Country each town of " 12 " requirements of plan China and above domestic refuse must be carried out harmless treatment, to there is the percolate that produces in a large amount of domestic rubbish disposal processes to process, because the custom of China's dietetic life causes the domestic refuse composition comparatively complicated, the percolate of its generation belongs to high organism, high salinity, high ammonia nitrogen and highly toxic waste water, be one of the most unmanageable waste water of generally acknowledging, make China's percolate be acknowledged as the most complicated and the most unmanageable waste water in the whole world.And the old standard of pollution control ratio of new standard " consumer waste filling and embedding pollutent control criterion " (GB168 89-2008) is more strict, cleanup standard is higher, especially increase the total nitrogen index, make and must the treatment process of percolate be improved, result is to cause whole treating processes more and more longer, worse and worse, operational management is more and more difficult for reliability, and cost and cost are also more and more higher.
From China's refuse leachate treatment technology development of nearly ten years, formed two kinds of main treatment process at present, a class is " biochemistry+film " technique, its flow process is seen shown in accompanying drawing 1; Another kind of is " MVC evaporation+ion-exchange " technique, sees that the patent No. is the Chinese patent (publication number is 101182083) of ZL200710031584.9, and its flow process is seen shown in accompanying drawing 2.
Because belonging to, percolate contains high strength ammonia waste water (500-2500mg/l), to this, country promulgates new landfill percolate processing emission standard " consumer waste filling and embedding pollutent control criterion " (GB168 89-2008), and this standard has increased the total nitrogen of discharging and controlled index (less than 40mg/l).For reaching These parameters, each treatment technology is all carried out further research round the removal of ammonia, problem up to standard.Research is found, just must increase new treating processes and strengthen each link strength disposal on the original base of above-mentioned treatment process, and this will cause rolling up of processing cost and management difficulty.
The main method that increases has stripping absorption, biological nitration and denitrification+reverse osmosis membrane, and MVC evaporation+ion-exchange etc.Wherein,
The ammonia of " stripping absorption " technology absorbs waste liquid and contains large amount of organic and other volatile matter, and it is difficult that processing disposal difficulty is large, expense is high, absorption liquid is disposed.
" biological nitration and denitrification+reverse osmosis membrane " technology can be comparatively thorough ammonia nitrogen removal, but construction investment is large, and management expectancy is high, and running cost is high, is prone to discharge beyond standards or systemic breakdown when operational management is not in place.
" MVC evaporation+ion-exchange " technology utilizes ion exchange resin that the ammonia in evaporation condensed water is adsorbed, ion exchange resin is by the regeneration of hydrochloric acid, form the ammonium chloride regeneration waste liquid, regeneration waste liquid adopts special-purpose ammonium chloride to concentrate and crystallizer, realize the recovery of ammonium chloride, facts have proved, this technology can realize the recovery of garbage filter liquefied ammonia, but its running cost is still higher, reach 13 yuan/tons of water (resin consumes 6 yuan/tons of water of 2 yuan/tons of water+ammonium chloride crystals of 5 yuan/tons of water+hydrochloric acid), in addition, the ammonia recovery system need adopt full titanium material to make, and manufacturing cost is high.Therefore above-mentioned technology is not suitable for the project implementation that scale is less, the recyclable amount of ammonia is little.
In above-mentioned treatment process, the efficiency that improves vaporizer is a key that reduces processing cost and improve processing efficiency.At present the function of vaporizer is concentrated waste water or produces steam, and vaporizer divides 3 kinds of normal pressure, pressurization and decompressions by working pressure.Moving situation by solution in vaporizer divides to be had:
1. circular form: boiling solution is the Multiple through then out heating surface in evaporator room, as central circulation tubular type, an outstanding basket formula, external-heat, Lie Wenshi and forced cyclic type etc.
2. one way type: boiling solution, once by heating surface, does not circulate in evaporator room, discharge at once concentrated solution, as rise membrane type, falling film type, stirring film type and centrifugal thin-film formula etc.
3. direct contact-type: heating medium and solution direct contact heat transfer, as submerged combustion evaporator.
Evaporation unit in operating process, consume a large amount of heating steams,, for saving heating steam, can adopt multi-effect evaporating device and vapor recompression vaporizer.Different evaporated forms are in order to adapt to different water quality, the fouling as whether easily? whether concentrated solution thickness? can crystallization? how is thermo-sensitivity? boiling point rises, cooling degenerative condition etc., the change of variety of way is all how can be concentrated to smoothly higher concentration ratio in order to solve, current cost after reducing.In addition, how the secondary steam by producing after evaporation process being purified, is also a difficult problem in existing treatment process.What research was more at present is the demist net of enhanced water evaporation device, and the salinity of minimizing steam is carried the impact on follow-up equipment secretly.but can be in waste water evaporative distillation water method direct up to standard, general all by back, add again the segment process process distilled water that condensation forms to secondary steam and carry out water treatment and solve, as adopt biochemistry, or ion-exchange, or strong oxidation, the techniques such as stripping, as disclosed in Chinese invention patent 200710031584.9 " a kind for the treatment of process of percolate " is exactly to add that the subsequent treatment process such as ion-exchange solve distilled water ammonia nitrogen high-content problem after to the waste water evaporation process, this just makes existing treatment process become increasingly complex, treating processes is more and more longer, cost is also more and more higher.
Therefore, need badly a kind of efficient, fast, low-cost, the simple method for treating garbage percolation liquid of operational management reclaims and reaches the emission request of percolate to realize ammonia.
Summary of the invention
First purpose of the present invention is to provide a kind of can carry out the percolate evaporation concentration treatment process that ammonia reclaims, the method is carried out evaporation process to percolate or the high organism high-salt wastewater of high ammonia, make ammonia and volatile organic matter evaporation wherein and with water vapor, form secondary steam, in the secondary steam flow process, ammonia is reclaimed and with organic matter removal, make the distilled water after processing meet in the situation of relevant emission standards, also have the characteristics thorough, easy to implement that absorb.
Second goal of the invention of the present invention is to provide a kind of described equipment that can carry out the percolate evaporation concentration treatment process of ammonia recovery that uses, this simple in equipment, and have low cost of manufacture, stable, be easy to manage, characteristics that processing efficiency is high, it can realize can solving the purification of percolate or the high organism high-salt wastewater of high ammonia and the purpose that ammonia reclaims by an equipment.
First purpose of the present invention can realize by following technical measures:
A kind of percolate evaporation concentration treatment process that can carry out the ammonia recovery comprises following treating processes:
(1) evaporator room of percolate being sent in vaporizer carries out the evaporation concentration processing, forms secondary steam and concentrated solution;
(2) secondary steam that step (1) is produced carries out the ammonia recycling: with the absorbing ammonia recovery and treatment method, described secondary steam is done the ammonia recycling in employing, specifically allow secondary steam pass through sour absorption liquid, thereby carry out neutralization reaction, separate out ammonium salt, the secondary steam after neutralization reaction purifies continues to flow into next link;
(3) secondary steam after ammonia recycling is sent into by pipeline in heating tube in vaporizer in step (1), thermal source as the evaporation percolate, when percolate was carried out heating evaporation, the secondary steam after described purification was also carried out the liquid cooling distilled water that discharges up to standard that congeals into by percolate;
At least, to the secondary steam hyperthermic treatment of once pressurizeing, be used for promoting secondary steam and advance at pipeline in vapour line before above-mentioned secondary steam is condensed into distilled water.
The ammonia recovery and treatment method that neutralization of the present invention absorbs can be: will, for the described secondary steam of ammonia restored acid absorption liquid spray, perhaps, secondary steam directly be passed in described sour absorption liquid.
Described sour absorption liquid can adopt one or more acid solutions in sulfuric acid or nitric acid or phosphoric acid to form, the pH value of described sour absorption liquid less than 4.5, temperature is higher than 0～5 ℃ of the temperature of secondary steam.
Pressurization hyperthermic treatment link in the vapour line of secondary steam of the present invention can be before the secondary steam in step (2) carries out ammonia recycling, perhaps after, arrange and all can respectively before and after perhaps.
The present invention can make following improvement: will be after ammonia recycling and the secondary steam before entering described heating tube further carry out again the oxidation of volatile matter/absorptions processing, in order to secondary steam is further purified.
The present invention can also make following improvement: the percolate of described step (1) is carrying out also carrying out pre-treatment before the evaporation concentration processing, described pre-treatment is one or more in precipitation process, filtration treatment, air supporting processing, degassed, the softening processing, thereby the tiny solid sundries in the described percolate of removal part and volatile organic matter etc., in order to avoid the shower nozzle in the obstruction vaporizer, the processing of reduction to volatile organic matter, reduce fouling, extend the cleaning interval of vaporizer.
Can also add the temperature and pressure measurement in the recycling of described ammonia and oxidation/absorptions treating processes, and by the temperature value that measures and the pressure in the described pressurization hyperthermic treatment process of force value control.
The concentrated solution of described percolate after evaporation concentration is processed is the 5-12% of the percolate before evaporation concentration is processed.
Second purpose of the present invention can realize by following technical measures:
A kind of be used to realizing first purpose percolate evaporation concentration treatment facility of the present invention, comprise vaporizer and vapour compressor, wherein, vaporizer comprises evaporator room, heating tube, it is characterized in that, on the vapour outlet that is communicated with described evaporator room and the pipeline between heating tube, the ammonia recovering mechanism is set; Described vapour outlet is connected with the steam-in of described ammonia recovering mechanism by the first pipeline, so that the secondary steam that evaporator room is evaporated is sent in described ammonia recovering mechanism; The vapour outlet of described ammonia recovering mechanism is connected with the steam-in of the heating tube of described vaporizer by the second pipeline; Described vapour compressor can be located on described the first pipeline and/or the second pipeline,, in order to the secondary steam high pressure in pipeline is heated up, promotes secondary steam and flows in each pipeline.
Treatment facility of the present invention can also comprise the oxidation/absorbing mechanism for the treatment of the volatile matter in secondary steam, and described oxidation/absorbing mechanism is arranged on described the second pipeline.
Vertical or the horizontal-type evaporator that vaporizer recommend adoption of the present invention is general.
The embodiment that the present invention recommends is: described ammonia recovering mechanism mainly is comprised of acid bath, deacidification part, steam inlet pipe, steam outlet pipe and the ammonium salt vent pipe of a sealing, described deacidification part is arranged on the front end of described steam outlet pipe, thereby removes the sour absorption liquid drop of carrying secretly in secondary steam; At the bottom of described ammonium salt vent pipe is located at the pond of described acid bath, and the mouth of pipe of ammonium salt vent pipe is provided with control valve; Described steam inlet pipe inserts in the sour absorption liquid of acid bath, so that described secondary steam directly passes in described acid bath while entering the ammonia recovering mechanism, then the secondary steam that passes from acid bath is discharged by steam outlet pipe through described deacidification part, and the ammonium salt of separating out after the ammonia in secondary steam and sour absorption liquid neutralization reaction is discharged described acid bath by described ammonium salt vent pipe.
Another embodiment that the present invention recommends is: described oxidation/absorbing mechanism is an enclosed housing, described cavity wall is provided with steam-in and vapour outlet, be provided with in described enclosed housing the activated carbon adsorption layer that cuts off described enclosed housing vertically is set, described steam-in and vapour outlet lay respectively on the enclosed housing of both sides of described activated carbon adsorption layer.
the present invention can also do following further improvement: described ammonia recovering mechanism and described oxidation/absorbing mechanism are that the ammonia recovery/oxidation that is combined into one absorbs integral mechanism, specifically, it is an enclosed housing that this ammonia recovery/oxidation absorbs integral mechanism, the sealing inside cavity is provided with acid bath, deacidification part and activated carbon adsorption layer, and the sealing cavity is provided with steam inlet pipe, steam outlet pipe and ammonium salt vent pipe, wherein, described activated carbon adsorption layer vertically arranges and cuts off described enclosed housing, described steam inlet pipe and steam outlet pipe lay respectively on the enclosed housing of both sides of described activated carbon adsorption layer, described acid bath is positioned at the enclosed housing of a side cavity at described steam inlet pipe place, and described steam inlet pipe inserts in the sour absorption liquid of acid bath, at the bottom of described ammonium salt vent pipe is located at the pond of described acid bath, described deacidification part is located on described acid bath and is tilted towards described activated carbon adsorption layer.
Also be provided with the photoelectrocatalysioxidization oxidization district in described enclosed housing.
The present invention contrasts prior art, has the following advantages:
1, to have changed in the concentrated treatment process of traditional percolate be all the thinking that phlegma for secondary steam purifies and ammonia recovery etc. is processed in the present invention, adoption of innovation directly carries out the reclaiming cleans such as ammonia recovery, gas delivery, oxidation, absorption to be processed secondary steam, the treatment process that again the secondary steam heat is reused, make the distilled water water quality of generation controlled, and discharging or reuse on request, treatment scheme is simple, easy handling is implemented.And equipment that be used for to implement the inventive method is an integrated device that solves the highly difficult wastewater treatment of high density, effectively replaces the processing of original complicated long flow process, makes that operation is easier, overall flow is easy to control;
2, the secondary steam after the purification in the present invention also is used for its heat of recycling: on the one hand the latent heat of vaporization of secondary steam is used for the evaporation of the follow-up percolate that adds; Percolate can make again the secondary steam after purification be condensed into the distilled water that can discharge on the other hand.Therefore more save heating cost, maximum amplitude reduces the impact on ambient atmosphere simultaneously;
3, compare with traditional treatment method, present method is owing to reducing ion-exchange unit and resin expense, exempted the processing of resin regeneration water, and the great expense that in reuse water, the condensing crystal of ammonium salt reclaims, so running cost reduces greatly, and because relevant device can directly adopt existing common equipment, it is low that equipment cost is also compared traditional method, compare with traditional evaporation+ion-exchange+crystallization processes, cost reduces 5-10%, and total operating cost reduces 18-25%;
4, in operational process of the present invention, the strength disposal of each processing links can be controlled as required at any time, for example according to the pressure and temperature data that detect in oxidation/absorption treating processes, the pressure in the pressure treatment process is regulated, to guarantee the normal operation of vapo(u)rization system; , according to organic concentration in steam, adjust oxidation absorption intensity and the residence time, in order to can control all the time water outlet quality up to standard;
5, the present invention not only can be used for the processing of percolate, can also be applied to the processing of similar trade effluent, makes industrial wastewater discharge reach related request.
Description of drawings
Fig. 1 is traditional " biological nitration and denitrification+reverse osmosis membrane " art breading schema;
Fig. 2 is traditional " MVC evaporation+ion-exchange " art breading schema;
Fig. 3 is specific embodiment one structural representation of percolate evaporation concentration treatment facility of the present invention;
Fig. 4 is specific embodiment two structural representations of percolate evaporation concentration treatment facility of the present invention;
Fig. 5 is specific embodiment three structural representations of percolate evaporation concentration treatment facility of the present invention;
Fig. 6 is the cross-sectional schematic of ammonia recovering mechanism in percolate evaporation concentration treatment facility of the present invention;
Fig. 7 is the cross-sectional schematic of oxidation/absorbing mechanism in percolate evaporation concentration treatment facility of the present invention;
Fig. 8 is the vertical view of ammonia recovery/oxidation-adsorption integral mechanism in percolate evaporation concentration treatment facility of the present invention;
Fig. 9 is the cross-sectional schematic of ammonia recovery/oxidation-adsorption integral mechanism shown in Figure 8.
Embodiment
Specific embodiment one
The percolate evaporation concentration equipment that can carry out the ammonia recovery shown in Figure 3 is one of embodiments of the invention, and this equipment comprises the unit such as vaporizer, vapour compressor, ammonia recovering mechanism and oxidation/absorbing mechanism; In the equipment of the present embodiment, vaporizer adopts the MVC horizontal-type evaporator, also can adopt existing general vertical-type evaporator.This horizontal-type evaporator comprises evaporator room, heating tube, on the vapour outlet of connection evaporator room and the pipeline between heating tube, the ammonia recovering mechanism is set; Vapour outlet is connected with the steam-in of ammonia recovering mechanism by the first pipeline, so that the secondary steam that evaporator room is evaporated is sent in the ammonia recovering mechanism; The vapour outlet of ammonia recovering mechanism is connected with the steam-in of the heating tube of vaporizer by the second pipeline; Vapour compressor has two: the first vapour compressor and the second vapour compressor, respectively establish one respectively on the first pipeline and the second pipeline, and, in order to the secondary steam high pressure in pipeline is heated up, promote secondary steam and flow in each pipeline.
In the present embodiment, as shown in Figure 6, the ammonia recovering mechanism mainly is comprised of acid bath 1, deacidification part 2, steam inlet pipe 4, steam outlet pipe 5 and the ammonium salt vent pipe 6 of a sealing, deacidification part 2 is arranged on the front end of steam outlet pipe 5, in this example, this deacidification part 2 directly adopts the demist net, also can directly adopt acid separator to replace the demist net, thereby removes the drop of the tiny sour absorption liquid of carrying secretly in secondary steam.at the bottom of ammonium salt vent pipe 6 is located at the pond of acid bath 1, the mouth of pipe is provided with control valve, steam inlet pipe 4 inserts in the sour absorption liquid of acid bath 1 downwards by the acid bath top, so that secondary steam directly passes in acid bath while entering the ammonia recovering mechanism, then the secondary steam that passes from acid bath is discharged by steam outlet pipe through the deacidification part, after a certain amount of ammonium salt of separating out after the ammonia in secondary steam and sour absorption liquid neutralization reaction, the ammonium salt vent pipe is opened and made ammonium salt discharge acid bath, because the sour absorption liquid of part also can be along with ammonium salt is discharged, therefore, in supplementing back again acid absorption liquid pool after the solid ammonium salt is removed in this part acid absorption liquid.Wherein the sour absorption liquid in acid bath adopts the mix acid liquor of sulfuric acid, nitric acid and phosphoric acid to form, the pH value of sour absorption liquid less than 4.5, temperature is higher than 0～5 ℃ of the temperature of secondary steam.Can certainly adopt the sour absorption liquid of wherein one or more compositions in sulfuric acid, nitric acid and phosphoric acid.
Wherein, ammonium salt is separated out mode and is reaction enrichment method crystallization in the ammonia absorption unit, and namely neutralization reaction constantly increases ammonium salt concentration, reaches crystallization and separates out, and crystalline ammonium salts is discharged the ammonia recovering mechanism again; Also can adopt the mode that partial concentration acid absorption liquid is carried out crystallisation by cooling in the mechanism outside to separate out ammonium salt.
As shown in Figure 7, oxidation/absorbing mechanism is an enclosed housing, cavity wall is provided with steam-in and vapour outlet, be provided with the activated carbon adsorption layer 3 that the exclusion seal cavity vertically is set in enclosed housing, steam-in and vapour outlet lay respectively on the enclosed housing of both sides of activated carbon adsorption layer, and wherein in a side cavity, the photoelectrocatalysioxidization oxidization device carries out photoelectrocatalysioxidization oxidization to secondary steam.Wherein activated carbon adsorption layer can directly adopt the absorption stopping composition such as gac.
in other embodiments, as shown in Figure 8 and Figure 9, this ammonia recovering mechanism and oxidation/absorbing mechanism can adopt the ammonia recovery/oxidation that is combined into one to absorb the structure formation of integral mechanism, specifically, it is an enclosed housing 7 that this ammonia recovery/oxidation absorbs integral mechanism, the sealing inside cavity is provided with acid bath 1, deacidification part 2 and activated carbon adsorption layer 3, and the sealing cavity is provided with steam inlet pipe 4, steam outlet pipe 5 and ammonium salt vent pipe 6, wherein, activated carbon adsorption layer 3 vertically arranges and cuts off sealing cavity 7, steam inlet pipe 4 and steam outlet pipe 5 lay respectively on the enclosed housing of both sides of activated carbon adsorption layer 3, acid bath 1 is positioned at the enclosed housing of a side cavity at steam inlet pipe 4 places, at the bottom of ammonium salt vent pipe 6 is located at the pond of acid bath, the mouth of pipe is provided with control valve, deacidification part 2 adopts the demist net, and is located on acid bath 1 and tilts towards activated carbon adsorption layer 3, and the cavity between acid bath 1 and activated carbon adsorption layer 3 is the photoelectrocatalysioxidization oxidization district.
Secondary steam enters in this integral mechanism, and the sour absorption liquid in ammonia and acid bath reacts, and when the ammonium salt concentration in sour absorption liquid reaches capacity, crystallization is formed the solid ammonium salt, and the solid ammonium salt is by outside the ammonium salt vent pipe discharger at the bottom of pond.The secondary steam that is absorbed after ammonia enters the photoelectrocatalysioxidization oxidization district by the deacidification part, is absorbed by activated carbon adsorption layer after organism is oxidized again, thereby makes steam be purified fully.In addition, as shown in Figure 8, this activated carbon adsorption layer 3 arranges respectively feed-pipe 31 and blow-off pipe 32 with the both sides that enclosed housing 7 joins, thereby can carry out regular replenishment filler and spray cleaning to this activated carbon adsorption layer 3, to guarantee adsorption effect.
In the present embodiment, but in ammonia recovering mechanism and oxidation/absorbing mechanism also set temperature and pressure transmitter, be used for measuring vapor temperature and force value, operator control the pressure of vapour compressor according to the temperature value that measures and force value.The temperature range of controlling that heats up is: 102 ℃ to 218 ℃, according to required vaporization temperature, determine.
Adopt said apparatus to carry out the percolate evaporation concentration and process, idiographic flow is as follows:
(1) at first percolate is carried out pre-treatment: pre-treatment comprises that specifically precipitation process, filtration treatment, air supporting are processed, degassed, the softening processing, thereby the tiny solid sundries in the described percolate of removal part and volatile organic matter etc., in order to avoid the shower nozzle in the obstruction vaporizer, the processing of reduction to volatile organic matter, reduce fouling, extend the cleaning interval of vaporizer.
(2) percolate after pretreated is sent in evaporator room in MVC formula vaporizer, carried out evaporation concentration and process, the concentrated solution that forms secondary steam and can discharge; If concentrated solution reaches concentrated ratio by concentrated solution outlet, discharges, in the present embodiment, the concentrated solution that can discharge is the 5-12% of the percolate before evaporation concentration is processed.Certainly go and discharge again after also can adjusting according to actual needs concentrated ratio.Then, secondary steam is sent in the first vapour compressor through the first pipeline by the vapour outlet of evaporator room, and the first compressor provides propulsive force for secondary steam, thereby makes secondary steam travel forward, and guarantees to pass into smoothly in the sour absorption liquid of next step;
(3) advancing secondary steam after the processed compressed of step (2) enters successively in ammonia recovering mechanism and oxidation/absorbing mechanism again and carries out ammonia recycling and oxidation/absorption processing, detailed process is: at first the secondary steam of being sent here by the first pipeline enters in acid bath and carries out neutralization reaction and separate out ammonium salt by steam inlet pipe, ammonium salt is discharged acid bath by the ammonium salt vent pipe of acid bath bottom, and the secondary steam after neutralization reaction purifies is emerged and sent into oxidation/absorbing mechanism through demist net and steam outlet pipe from the acid bath top again; At first secondary steam after purification enters the photoelectrocatalysioxidization oxidization district by steam-in,, again by activated carbon adsorption layer, discharges by vapour outlet finally after photoelectrocatalysioxidization oxidization; In the present embodiment, the steam residual ammonia concentration after the ammonia recycling requires to purify, less than 15mg/l, could be sent the secondary steam after processing into next step and process discharging.
(3) secondary steam after ammonia recycling and oxidation/absorption processing is sent in the second vapour compressor through the compression that again heats up by the second pipeline;
(4) secondary steam after the second vapour compressor compression is sent in heating tube in vaporizer in step (1) by the second pipeline again, thermal source as the evaporation percolate, when percolate was carried out heating evaporation, the secondary steam after purification also was condensed into the distilled water that discharges up to standard by percolate;
The ammonia recovery and treatment method adopts the mode that secondary steam is passed into acid bath in the present embodiment, can certainly adopt the mode of sour absorption liquid spray contact secondary steam.
During oxidation in the present embodiment/absorption is processed, method for oxidation adopts the photoelectrocatalysioxidization oxidization mode, can certainly adopt according to different organic components the methods such as plasma oxidation or the oxidation of carbon palladium.
In this device and flow processing process, thereby adopted two vapour compressors to pressurize to heat up to secondary steam, overcome the thermosteresis that ammonia reclaims and volatile matter is processed.Improve the temperature of secondary steam, be convenient to carrying out smoothly of subsequent processes.In addition, if effectively removed volatile matter in preprocessing process, perhaps the volatile matter in pretreated percolate has reached emission standard, this device and flow process also can be omitted oxidation/absorbing mechanism and corresponding treatment scheme, and concrete structure and flow process are seen specific embodiment two and three.
Specific embodiment two
The difference of the treatment facility of the percolate of the present embodiment and specific embodiment one is to have omitted oxidation/absorbing mechanism and the second vapour compressor, and its structural representation as shown in Figure 4.Its concrete treatment scheme is:
(1) at first the percolate after pretreated is sent in vaporizer, evaporation produces ammonia and volatile matter is discharged vaporizer in the lump with secondary steam;
(2) secondary steam enters in the ammonia recovering mechanism after entering the vapour compressor pressurization.
(3) after the sour absorption liquid in the ammonia in secondary steam and ammonia recovering mechanism carries out neutralization reaction, separate out ammonium salt, the acid absorption liquid keeps PH less than 4.5, control simultaneously sour absorption liquid temperature higher than secondary steam 0-5 ℃, thereby guarantee that steam does not participate in reaction and remains unchanged, the neutralization reaction mode requires to purify rear entrainment with steam ammonia concentration less than 15mg/l, ammonium salt concentration constantly increases, reach crystallization, crystalline ammonium salts is discharged the ammonia recovering mechanism, realizes reclaiming ammonia from steam;
(4) secondary steam is got back to vaporizer by the second pipeline and is evaporated percolate as thermal source, and secondary steam is condensed into distilled water simultaneously, and water quality can reach emission standard.
Specific embodiment three
The difference of the treatment facility of the percolate of the present embodiment and specific embodiment one is to omit the first vapour compressor and oxidation/absorbing mechanism, and its structural representation as shown in Figure 5.Concrete treatment scheme is:
(1) at first the percolate after pretreated is sent in vaporizer, evaporation produces ammonia and volatile matter is discharged vaporizer in the lump with secondary steam;
(2) the sour absorption liquid in the ammonia in secondary steam and ammonia recovering mechanism carries out neutralization reaction, separate out ammonium salt, the acid absorption liquid keeps PH less than 4.5, control simultaneously sour absorption liquid temperature higher than secondary steam 0-5 ℃, thereby guarantee that steam does not participate in reaction and remains unchanged, the neutralization reaction mode requires to purify rear entrainment with steam ammonia concentration less than 15mg/l, ammonium salt concentration constantly increases, reach crystallization, crystalline ammonium salts is discharged the ammonia recovering mechanism, realizes reclaiming ammonia from steam; Ammonia and the heat production of acid-respons process, can keep steam when being cleaned, and its heat energy does not reduce, and keeps the steady running of vapo(u)rization system;
(3) secondary steam of deammoniation heats up through the second vapour compressor compression, get back to vaporizer and evaporate percolate as thermal source, and vapor condensation becomes distilled water, and water quality can reach emission standard or do simple processing qualified discharge.
Embodiments of the present invention are not limited to this; under the above-mentioned basic fundamental thought of the present invention prerequisite; according to modification, replacement or the change to other various ways that content of the present invention is made of the ordinary skill knowledge of this area and customary means, within all dropping on rights protection scope of the present invention.
Claims (2)
1. one kind can be carried out the percolate evaporation concentration treatment process that ammonia reclaims, and it is characterized in that comprising following treating processes:
(1) evaporator room of percolate being sent in vaporizer carries out the evaporation concentration processing, forms secondary steam and concentrated solution;
(2) secondary steam that step (1) is produced carries out the ammonia recycling: with the absorbing ammonia recovery and treatment method, described secondary steam is done the ammonia recycling in employing, specifically allow secondary steam directly pass into sour absorption liquid, the pH value of described sour absorption liquid is less than 4.5, temperature is higher than 0～5 ℃ of the temperature of secondary steam, thereby carry out neutralization reaction, separate out ammonium salt, the secondary steam after neutralization reaction purifies continues to flow into next link;
(3) secondary steam after ammonia recycling is sent into by pipeline in heating tube in vaporizer in step (1), thermal source as the evaporation percolate, when percolate was carried out heating evaporation, the secondary steam after described purification was also carried out the liquid cooling distilled water that discharges up to standard that congeals into by percolate;
In vapour line before above-mentioned secondary steam is condensed into distilled water at least to the secondary steam hyperthermic treatment of once pressurizeing, the temperature range that heats up and control: 102 ℃ to 218 ℃, be used for promoting secondary steam and advance at pipeline;
Add temperature and pressure and measure in described ammonia recycling treating processes, and by the temperature value that measures and force value, control pressure in described pressurization hyperthermic treatment process.
2. percolate evaporation concentration treatment process according to claim 1 is characterized in that: the pressurization hyperthermic treatment link in the vapour line of described secondary steam is that the secondary steam in step (2) carries out arranging respectively before and after the ammonia recycling.
3. percolate evaporation concentration treatment process according to claim 1 and 2 is characterized in that: will be after the ammonia recycling and the secondary steam before entering described heating tube further carry out again the oxidation of volatile matter/absorptions processing.
4. percolate evaporation concentration treatment process according to claim 3, it is characterized in that: the percolate of described step (1) is carrying out also carrying out pre-treatment before the evaporation concentration processing, and described pre-treatment is one or more in precipitation process, filtration treatment, air supporting processing, degassed, the softening processing.
5. percolate evaporation concentration treatment process according to claim 4, it is characterized in that: add temperature and pressure in described oxidation/absorption treating processes and measure, and by the temperature value that measures and force value, control pressure in described pressurization hyperthermic treatment process.
6. equipment that is used for realizing described any percolate evaporation concentration treatment process of claim 1～5, comprise vaporizer and vapour compressor, wherein, vaporizer comprises evaporator room, heating tube, it is characterized in that, on the vapour outlet that is communicated with described evaporator room and the pipeline between heating tube, the ammonia recovering mechanism is set, described ammonia recovering mechanism is mainly by an acid bath that seals, the deacidification part, steam inlet pipe, steam outlet pipe and ammonium salt vent pipe form, described deacidification part is arranged on the front end of described steam outlet pipe, at the bottom of described ammonium salt vent pipe is located at the pond of described acid bath, and the mouth of pipe of ammonium salt vent pipe is provided with control valve, described steam inlet pipe inserts in the acid solution of acid bath, described vapour outlet is connected with the steam-in of described ammonia recovering mechanism by the first pipeline, and the vapour outlet of described ammonia recovering mechanism is connected with the steam-in of the heating tube of described vaporizer by the second pipeline, described vapour compressor is located on described the first pipeline and/or the second pipeline, also be provided with the temperature and pressure sensor in the ammonia recovering mechanism, be used for measuring vapor temperature and force value.
7. equipment according to claim 6, it is characterized in that: it also comprises the oxidation/absorbing mechanism for the treatment of the volatile matter in secondary steam, described oxidation/absorbing mechanism is arranged on described the second pipeline.
8. equipment according to claim 7, it is characterized in that: described oxidation/absorbing mechanism is an enclosed housing, described cavity wall is provided with steam-in and vapour outlet, be provided with the activated carbon adsorption layer that the exclusion seal cavity vertically is set in described enclosed housing, described steam-in and vapour outlet lay respectively on the enclosed housing of both sides of described activated carbon adsorption layer.
9. according to claim 7 or 8 described equipment, it is characterized in that: described ammonia recovering mechanism and described oxidation/absorbing mechanism are that the ammonia recovery/oxidation that is combined into one absorbs integral mechanism, specifically, it is an enclosed housing that this ammonia recovery/oxidation absorbs integral mechanism, the sealing inside cavity is provided with acid bath, deacidification part and activated carbon adsorption layer, and the sealing cavity is provided with steam inlet pipe, steam outlet pipe and ammonium salt vent pipe, wherein, described activated carbon adsorption layer vertically arranges and cuts off described enclosed housing, described steam inlet pipe and steam outlet pipe lay respectively on the enclosed housing of both sides of described activated carbon adsorption layer, described acid bath is positioned at the enclosed housing of a side cavity at described steam inlet pipe place, and in the sour absorption liquid in described steam inlet pipe insertion acid bath, at the bottom of described ammonium salt vent pipe is located at the pond of described acid bath, described deacidification part is located on described acid bath and is tilted towards described activated carbon adsorption layer.
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| CN102838180B (en) * | 2012-08-16 | 2014-11-12 | 广州新普利节能环保科技有限公司 | Rare metal wastewater zero discharge process |
| CN102838244A (en) * | 2012-08-16 | 2012-12-26 | 广州新普利节能环保科技有限公司 | Landfill leachate treatment process and device |
| CN102826701B (en) * | 2012-08-23 | 2014-04-09 | 李虹 | Method for deep purification of leachate by using single factor separation |
| CN105126574B (en) * | 2015-07-24 | 2018-06-26 | 中山沃尔威多水处理设备有限公司 | A kind of evaporator steaming is except ammonia and ammonium salt reclamation vapo(u)rization system and technique |
| CN105906124A (en) * | 2016-06-02 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | System and method for recycling landfill leachate ammonia nitrogen |
| CN107827291A (en) * | 2017-09-26 | 2018-03-23 | 上海晶宇环境工程股份有限公司 | Percolate reverse osmosis concentration liquor treating process and special equipment |
| CN113023994B (en) * | 2021-03-18 | 2024-04-26 | 河南绿水青山环保科技有限公司 | Chemical wastewater treatment and recycling device |
| CN114538675A (en) * | 2022-01-11 | 2022-05-27 | 安徽普朗膜技术有限公司 | Landfill leachate treatment system and treatment method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001012548A1 (en) * | 1999-08-11 | 2001-02-22 | Hadwaco Ltd Oy | Method for the evaporation of an aqueous solution containing ammonia |
| JP2006239578A (en) * | 2005-03-03 | 2006-09-14 | Kurita Water Ind Ltd | Ammonia nitrogen and soluble salt-containing water treatment apparatus and method |
| CN101182049A (en) * | 2007-11-23 | 2008-05-21 | 陈伟雄 | Evaporation system for treating refuse leachate |
| CN201343459Y (en) * | 2009-01-23 | 2009-11-11 | 华南理工大学 | Heat energy conversion device for heating garbage percolate |
| CN102030386A (en) * | 2010-10-15 | 2011-04-27 | 北京化工大学 | Efficient energy-saving coupling stripping deamination equipment and method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202284169U (en) * | 2011-09-09 | 2012-06-27 | 陈伟雄 | Landfill leachate evaporation concentration apparatus capable of recovering ammonia |
-
2011
- 2011-09-09 CN CN2011102671469A patent/CN102358625B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001012548A1 (en) * | 1999-08-11 | 2001-02-22 | Hadwaco Ltd Oy | Method for the evaporation of an aqueous solution containing ammonia |
| JP2006239578A (en) * | 2005-03-03 | 2006-09-14 | Kurita Water Ind Ltd | Ammonia nitrogen and soluble salt-containing water treatment apparatus and method |
| CN101182049A (en) * | 2007-11-23 | 2008-05-21 | 陈伟雄 | Evaporation system for treating refuse leachate |
| CN201343459Y (en) * | 2009-01-23 | 2009-11-11 | 华南理工大学 | Heat energy conversion device for heating garbage percolate |
| CN102030386A (en) * | 2010-10-15 | 2011-04-27 | 北京化工大学 | Efficient energy-saving coupling stripping deamination equipment and method |
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