CN104743728A - Energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water - Google Patents
Energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water Download PDFInfo
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Abstract
The invention relates to an energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water. The method comprises the following steps: transporting the surplus ammonia water to a liquid distributor on the upper part of a deaminizing tower stripping section, and flowing through a stripping section filling layer from top to bottom; heating the surplus ammonia water by the after heat of an enterprise cyclic dilute ammonia water, returning to the deaminizing tower and evaporating under the negative pressure of 20-28 KPa to generate a secondary vapor; passing the secondary vapor through the stripping section filling layer from top to bottom to contact with the reversely flown surplus ammonia water and deaminizing the surplus ammonia water; when the surplus ammonia water reaches the tower bottom to become standard surplus ammonia water, extracting out form the tower; when the secondary vapor reaches the top of the deaminizing tower, absorbing most ammonia, bringing out from the deaminizing tower, coming into a condenser, introducing the ammonia mixed gas extracted from the condenser to an ammonia absorbing tower, performing recycled absorbing by desalted water, generating 10-20% stronger ammonia water, transporting to a stronger ammonia water storage tank for use or for sale, refluxing the dilute ammonia water condensed by the condenser to the tower and further deaminizing.
Description
Technical field
The invention belongs to the field of waste water treatment of the chemical industries such as Coal Chemical Industry, new forms of energy chemical industry, petrochemical complex, be specifically related to the energy-saving deamination method adopting negative pressure deamination containing the residual coking ammonia water of ammonia, and the method for comprehensive utilization of the ammonia removing out.
Background technology
The chemical enterprises such as Coal Chemical Industry are in the cooling and washing process of coke production and gasification, form a large amount of weak ammonias containing ammonia, phenol, prussiate, sulfide, after this effluent part removes coal dust, coal dust, tar, use at system internal recycle as water coolant, be called cyclic ammonia water; Along with the increase of cycle index, the objectionable constituent enrichments such as ammonia nitrogen, regularly must discharge a part, supplementary portion division technique water purification simultaneously, cyclic ammonia water could normal circulation use, this part ammoniacal liquor of discharging is called remained ammonia, first will carry out deamination, then the Waste Water Treatment of Entry Firm could carry out in-depth and process.Deamination process at present to this part remained ammonia, major part enterprise adopts high temperature ammonia distillation process, and waste water is heated to 102-105 DEG C, and with the raw steam of high temperature, by ammonia nitrogen, from waste water, stripping is out, after being condensed into clean weak ammonia, for desulfurization or extracting sulfuric acid ammonium.This process characteristic is that energy consumption is high, and often process 1 ton of remained ammonia, only ammonia still process link steam expends just up to 150 kilograms, by the steam price of 120 yuan/kilogram, and expense 15 yuan.By the wet quenching coal chemical enterprise producing 2200000 tons, coke per year, the remained ammonia total amount of a year about 480,000 tons, raw expending of steam reaches 7,200,000 yuan, is a white elephant to enterprise.The cyclic ammonia water temperatures as high 72-80 DEG C of enterprise simultaneously, need more cold to cool and just can recycle, heat is wasted, and also will increase the investment of cooling infrastructure simultaneously.Along with downslide and national energy-saving, the enforcement of environmental protection new-standard and the increasing of supervision of Business Economic Benefit, try to explore new deamination method and treatment process, under the prerequisite meeting national environmental standard, realize energy-saving and cost-reducing and comprehensive utilization of resources, become the important and eager task of above-mentioned enterprise and scientific research institution.
Therefore, Coal Chemical Industry equal energy source, chemical enterprise, be badly in need of a kind of method, the Ammonia recovery in remained ammonia can be utilized, greatly can reduce again steam equal energy source and expend, realize comprehensive utilization of resources and energy conservation; Invest rather moderate simultaneously, and realize as far as possible running positive income.Only in this way, the long-term health development of Coal Chemical Industry equal energy source, chemical enterprise could be ensured.
Summary of the invention
The object of this invention is to provide a kind of energy-saving deamination method of residual coking ammonia water negative pressure deamination, the further biochemical treatment requirement of enterprise can be reached completely after making remained ammonia deamination, and ammonia is reclaimed, produce the ammoniacal liquor of 10-20% concentration, simultaneously complete in steam, realize UTILIZATION OF VESIDUAL HEAT IN and comprehensive utilization of resources, thus turn waste into wealth, the final raising quality of production, promotes Social and economic benef@.
For achieving the above object, the scheme that the present invention adopts is: a kind of energy-saving deamination method of residual coking ammonia water negative pressure deamination: comprise the following steps:
A, the remained ammonia in waste water workshop enters waste water cache pool, temperature 70-75 DEG C, remained ammonia pH value is after filtering adjusted between 11.5-12, be delivered to the liquid distributor on deammoniation tower (1) stripping section top through deammoniation tower opening for feed by deammoniation tower fresh feed pump (2), stripping section packing layer is flow through from top to bottom after cloth liquid, deammoniation tower (1) internal pressure only has absolute pressure 20-28KPa, remained ammonia evaporation 1.5-1.8%, temperature decreases 60-65 DEG C, after arriving deammoniation tower (1) bottom, interchanger (4) cold feed side is delivered to through interchanger (4) cold feed entrance by recycle pump (3), temperature 72-77 DEG C of circulation weak ammonia is delivered to interchanger (4) hot feed side by cyclic ammonia water recycle pump through interchanger (4) hot feed entrance,
Remained ammonia, cyclic ammonia water are through interchanger (4) indirect heat exchange, and cyclic ammonia water temperature is down to 63-68 DEG C, and heat constantly passes to remained ammonia, and remained ammonia temperature rises to 68-73 DEG C by 60-65 DEG C; Remained ammonia flows back to deammoniation tower (1) bottom again through interchanger (4) outlet, and tower internal pressure only has absolute pressure 20-28KPa, corresponding saturated steam temperature 60-65 DEG C, and remained ammonia constantly evaporates generation secondary steam; Secondary steam is from bottom to top through stripping section packing layer, and contact with the remained ammonia flowed from top to bottom is reverse, ammonia is constantly overflowed from remained ammonia, enters in secondary steam;
When remained ammonia arrives at the bottom of tower, by stripping out, according to different requirement, in remained ammonia, ammonia level only has 5-200mg/L to the ammonia overwhelming majority; Satisfactory remained ammonia is extracted out in tower by deammoniation tower (1) discharging pump (5), is delivered to enterprise's next procedure in-depth process;
When B, secondary steam arrive deammoniation tower (1) stripping section top, absorb most of ammonia, continue upwards to enter deammoniation tower (1) rectifying section, and the condensation weak ammonia of deammoniation tower (1) external reflux counter current contact between rectifying section filler, again the ammonia in backflow weak ammonia is absorbed, then from deammoniation tower (1) Base top contact, condenser (6) is entered;
In condenser (6), the contain ammonia secondary steam of recirculated cooling water to deammoniation tower (1) Base top contact of temperature 27-30 DEG C carries out condensation cooling, own temperature rises to 37-40 DEG C, discharges, enter cooling tower and carry out circulating cooling from condenser (6);
For ensureing that in deammoniation tower (1), pressure maintains the pressure-reduction level of 20-28KPa, water-ring vacuum pump (7) is set, with the shell side UNICOM of the side at condenser (6) secondary steam place, constantly the non-condensable gas in condenser (6) is extracted out, because condenser (6) shell side is by secondary steam pipeline and the direct UNICOM of deammoniation tower, thus in making deammoniation tower (1), pressure maintains the fixing horizontal of 20-28KPa;
C, secondary steam are recycled water coolant indirect condensing in condenser (6), and temperature is down to 50-60 DEG C, and most of secondary steam is condensed, and a part of ammonia is absorbed by secondary steam water of condensation, form weak ammonia; Whole weak ammonias that condensation is got off are delivered to deammoniation tower (1) rectifying section top through weak ammonia reflux pump (14), flow from top to bottom after cloth liquid, contact with the secondary steam risen from stripping section is reverse, major part ammonia is overflowed from weak ammonia, transfer in secondary steam, when arriving stripping section top liquid distributor, ammonia level wherein reaches balance with ammonia level in the remained ammonia entering deammoniation tower (1) stripping section top, carries out deamination through stripping section downwards together after the two mixing;
The noncondensable gas be not condensed of condenser (6) shell side is constantly extracted out by vacuum pump (7); Vacuum pump (7) and the direct UNICOM of ammonia absorber (8) hypomere, the ammonia gas mixture of extraction introduces ammonia absorber (8) hypomere first order absorption pars infrasegmentalis by vacuum pump;
D, ammonia absorber (8) point two sections: hypomere is first order absorption section, and epimere is secondary absorber portion, adopt de-salted water to absorb; According to ammonia level in remained ammonia and the concentration requirement reclaiming ammoniacal liquor, by de-salted water spray pump, de-salted water is quantitatively transferred to ammonia absorber (8) top, secondary absorber portion packing layer upper strata is evenly sprayed onto by nozzle, flow through secondary absorber portion packing layer from top to bottom, secondary absorption is carried out to unabsorbed ammonia after first order absorption section absorbs; De-salted water becomes weak ammonia after absorbing ammonia, continues to be downward through first order absorption section packing layer, carries out first order absorption to the ammonia gas mixture introduced from ammonia absorber (8) bottom; In absorption process, weak ammonia concentration improves constantly;
Consider in ammonia absorption process and discharge a large amount of heats, ammonia absorber (8) height is set up, weak ammonia and the part ammonia of bottom, absorption tower (8) flow out naturally from tower base cone body mouth, enter ammoniacal liquor water cooler (10), the recirculated cooling water of cooled device shell side is cooled to 35-40 DEG C indirectly, along with temperature reduces, ammonia is absorbed further by weak ammonia, and then gravity flow enters weak ammonia tank (11);
Concentration requirement is not reached for preventing a cyclic absorption ammonia concn, first order absorption circulated sprinkling pump (9) is set, weak ammonia is delivered to ammonia absorber (8) first order absorption section top from weak ammonia tank (11), first order absorption section packing layer upper strata is evenly sprayed onto by nozzle, together with the weak ammonia that secondary absorber portion flows down, as the absorption liquid of first order absorption section, cyclic absorption is carried out to the ammonia gas mixture passed by bottom, absorption tower from top to bottom;
When weak ammonia tank (11) ammonia concn reaches requirement, be delivered to by qualified aqua ammonia pump (12) that strong aqua storage tank (13) is for subsequent use or standby to be sold.
Principal feature of the present invention is: one is under the condition of low-temperature negative-pressure, the heat that carries with cyclic ammonia water heating remained ammonia, and the secondary steam of generation as the medium of stripping deamination, thus replaces raw steam completely; Two is possess the comparatively better removal effect of normal pressure deamination, according to enterprise's needs, and can by the ammonia nitrogen removal in remained ammonia to 5-200mg/L; Three is that the ammonia deviate from is directly used in the strong aqua producing concentration 10-20%, for enterprise's desulfurization or directly externally sale; Four is saved the equipment and energy consumption that to be carried out by cyclic ammonia water lowering the temperature.The comprehensive treating process that the method can be used for similar waste water utilizes.
Accompanying drawing explanation
Fig. 1 is embodiment of the present invention experimental installation structural representation.
Embodiment:
An energy-saving deamination method for residual coking ammonia water negative pressure deamination, comprises the following steps:
A, the remained ammonia in waste water workshop enters waste water cache pool, temperature 70-75 DEG C, remained ammonia pH value is after filtering adjusted between 11.5-12, pH value is adjusted between 11.5-12, and remained ammonia after filtering, temperature 70-75 DEG C, be delivered to the liquid distributor on deammoniation tower (1) stripping section top through deammoniation tower opening for feed by deammoniation tower fresh feed pump (2), stripping section packing layer is flow through from top to bottom after cloth liquid, because deammoniation tower (1) internal pressure only has 20-28KPa (absolute pressure, lower same)), a remained ammonia evaporation part (1.5-1.8%), temperature decreases 60-65 DEG C, after arriving deammoniation tower (1) bottom, interchanger (4) cold feed side is delivered to through interchanger (4) cold feed entrance by recycle pump (3), circulation weak ammonia (temperature 72-77 DEG C) is delivered to interchanger (4) hot feed side by cyclic ammonia water recycle pump through interchanger (4) hot feed entrance,
Remained ammonia, cyclic ammonia water are through interchanger (4) indirect heat exchange, and cyclic ammonia water temperature is down to 63-68 DEG C, and heat constantly passes to remained ammonia, and remained ammonia temperature rises to 68-73 DEG C by 60-65 DEG C; Remained ammonia flows back to deammoniation tower (1) bottom again through interchanger (4) outlet, because tower internal pressure only has 20-28KPa, and corresponding saturated steam temperature 60-65 DEG C, remained ammonia constantly evaporates generation secondary steam; Secondary steam is from bottom to top through stripping section packing layer, and contact with the remained ammonia flowed from top to bottom is reverse, ammonia is constantly overflowed from remained ammonia, enters in secondary steam;
When remained ammonia arrives at the bottom of tower, by stripping out, according to different requirement, in remained ammonia, ammonia level only has 5-200mg/L to the ammonia overwhelming majority; Satisfactory remained ammonia is extracted out in tower by deammoniation tower (1) discharging pump (5), is delivered to enterprise's next procedure in-depth process;
When B, secondary steam arrive deammoniation tower (1) stripping section top, absorb most of ammonia, continue upwards to enter deammoniation tower (1) rectifying section, and the condensation weak ammonia of deammoniation tower (1) external reflux counter current contact between rectifying section filler, again the ammonia in backflow weak ammonia is absorbed, then from deammoniation tower (1) Base top contact, condenser (6) is entered.
In condenser (6), the contain ammonia secondary steam of recirculated cooling water to deammoniation tower (1) Base top contact of temperature 27-30 DEG C carries out condensation cooling, own temperature rises to 37-40 DEG C, discharges, enter cooling tower and carry out circulating cooling from condenser (6);
For ensureing that in deammoniation tower (1), pressure maintains the pressure-reduction level of 20-28KPa, water-ring vacuum pump (7) is set, with condenser (6) shell side (side at secondary steam place) UNICOM, constantly the non-condensable gas in condenser (6) is extracted out, because condenser (6) shell side is by secondary steam pipeline and the direct UNICOM of deammoniation tower, thus in making deammoniation tower (1), pressure maintains the fixing horizontal of 20-28KPa;
C, secondary steam are recycled water coolant indirect condensing in condenser (6), and temperature is down to 50-60 DEG C, and most of secondary steam is condensed, and a part of ammonia is absorbed by secondary steam water of condensation, form weak ammonia; Whole weak ammonias that condensation is got off are delivered to deammoniation tower (1) rectifying section top through weak ammonia reflux pump (14), flow from top to bottom after cloth liquid, contact with the secondary steam risen from stripping section is reverse, major part ammonia is overflowed from weak ammonia, transfer in secondary steam, when arriving stripping section top liquid distributor, ammonia level wherein reaches balance with ammonia level in the remained ammonia entering deammoniation tower (1) stripping section top, carries out deamination through stripping section downwards together after the two mixing;
The noncondensable gas (ammonia gas mixture, mainly ammonia, containing a small amount of water vapor and other noncondensable gas of trace) be not condensed of condenser (6) shell side is constantly extracted out by vacuum pump (7); Vacuum pump (7) and the direct UNICOM of ammonia absorber (8) hypomere, the ammonia gas mixture of extraction introduces ammonia absorber (8) hypomere first order absorption pars infrasegmentalis by vacuum pump;
D, ammonia absorber (8) point two sections: hypomere is first order absorption section, and epimere is secondary absorber portion, adopt de-salted water to absorb.According to ammonia level in remained ammonia and the concentration requirement reclaiming ammoniacal liquor, by de-salted water spray pump, de-salted water is quantitatively transferred to ammonia absorber (8) top, secondary absorber portion packing layer upper strata is evenly sprayed onto by nozzle, flow through secondary absorber portion packing layer from top to bottom, secondary absorption is carried out to unabsorbed ammonia after first order absorption section absorbs; De-salted water becomes weak ammonia after absorbing ammonia, continues to be downward through first order absorption section packing layer, carries out first order absorption to the ammonia gas mixture introduced from ammonia absorber (8) bottom; In absorption process, weak ammonia concentration improves constantly;
Consider in ammonia absorption process and discharge a large amount of heats, ammonia absorber (8) height is set up, weak ammonia bottom absorption tower and part ammonia flow out naturally from tower base cone body mouth, enter ammoniacal liquor water cooler (10), the recirculated cooling water of cooled device shell side is cooled to 35-40 DEG C indirectly, along with temperature reduces, ammonia is absorbed further by weak ammonia, and then gravity flow enters weak ammonia tank (11);
Concentration requirement is not reached for preventing a cyclic absorption ammonia concn, first order absorption circulated sprinkling pump (9) is set, weak ammonia is delivered to ammonia absorber (8) first order absorption section top from weak ammonia tank (11), first order absorption section packing layer upper strata is evenly sprayed onto by nozzle, together with the weak ammonia that secondary absorber portion flows down, as the absorption liquid of first order absorption section, cyclic absorption is carried out to the ammonia gas mixture passed by bottom, absorption tower from top to bottom.
When weak ammonia tank (11) ammonia concn reaches requirement, be delivered to by qualified aqua ammonia pump (12) that strong aqua storage tank (13) is for subsequent use or standby to be sold.
Major equipment of the present invention comprises:
1, negative pressure stripping deamination and bootstrap system: be made up of deammoniation tower, interchanger, fresh feed pump, discharging pump, recycle pump, vacuum pump;
2, ammoniacal liquor preparation system: be made up of condenser, weak ammonia reflux pump, ammonia absorber, ammoniacal liquor water cooler, circulated sprinkling pump, qualified aqua ammonia pump, weak ammonia tank, strong aqua tank.
3, electrically, blind controller system: be made up of electrical system, DCS Controlling System and by-pass valve control, control instruments etc.
In the present invention, deamination institute heat requirement, all by self waste heat for supplying of systemic circulation ammoniacal liquor, substitutes outside raw steam heating completely; System itself is without feed enrichment problem.
Claims (1)
1. an energy-saving deamination method for residual coking ammonia water negative pressure deamination, is characterized in that: comprise the following steps:
A, the remained ammonia in waste water workshop enters waste water cache pool, temperature 70-75 DEG C, remained ammonia pH value is after filtering adjusted between 11.5-12, be delivered to the liquid distributor on deammoniation tower (1) stripping section top through deammoniation tower opening for feed by deammoniation tower fresh feed pump (2), stripping section packing layer is flow through from top to bottom after cloth liquid, deammoniation tower (1) internal pressure only has absolute pressure 20-28KPa, remained ammonia evaporation 1.5-1.8%, temperature decreases 60-65 DEG C, after arriving deammoniation tower (1) bottom, interchanger (4) cold feed side is delivered to through interchanger (4) cold feed entrance by recycle pump (3), temperature 72-77 DEG C of circulation weak ammonia is delivered to interchanger (4) hot feed side by cyclic ammonia water recycle pump through interchanger (4) hot feed entrance,
Remained ammonia, cyclic ammonia water are through interchanger (4) indirect heat exchange, and cyclic ammonia water temperature is down to 63-68 DEG C, and heat constantly passes to remained ammonia, and remained ammonia temperature rises to 68-73 DEG C by 60-65 DEG C; Remained ammonia flows back to deammoniation tower (1) bottom again through interchanger (4) outlet, and tower internal pressure only has absolute pressure 20-28KPa, corresponding saturated steam temperature 60-65 DEG C, and remained ammonia constantly evaporates generation secondary steam; Secondary steam is from bottom to top through stripping section packing layer, and contact with the remained ammonia flowed from top to bottom is reverse, ammonia is constantly overflowed from remained ammonia, enters in secondary steam;
When remained ammonia arrives at the bottom of tower, by stripping out, according to different requirement, in remained ammonia, ammonia level only has 5-200mg/L to the ammonia overwhelming majority; Satisfactory remained ammonia is extracted out in tower by deammoniation tower (1) discharging pump (5), is delivered to enterprise's next procedure in-depth process;
When B, secondary steam arrive deammoniation tower (1) stripping section top, absorb most of ammonia, continue upwards to enter deammoniation tower (1) rectifying section, and the condensation weak ammonia of deammoniation tower (1) external reflux counter current contact between rectifying section filler, again the ammonia in backflow weak ammonia is absorbed, then from deammoniation tower (1) Base top contact, condenser (6) is entered;
In condenser (6), the contain ammonia secondary steam of recirculated cooling water to deammoniation tower (1) Base top contact of temperature 27-30 DEG C carries out condensation cooling, own temperature rises to 37-40 DEG C, discharges, enter cooling tower and carry out circulating cooling from condenser (6);
For ensureing that in deammoniation tower (1), pressure maintains the pressure-reduction level of 20-28KPa, water-ring vacuum pump (7) is set, with the shell side UNICOM of the side at condenser (6) secondary steam place, constantly the non-condensable gas in condenser (6) is extracted out, because condenser (6) shell side is by secondary steam pipeline and the direct UNICOM of deammoniation tower, thus in making deammoniation tower (1), pressure maintains the fixing horizontal of 20-28KPa;
C, secondary steam are recycled water coolant indirect condensing in condenser (6), and temperature is down to 50-60 DEG C, and most of secondary steam is condensed, and a part of ammonia is absorbed by secondary steam water of condensation, form weak ammonia; Whole weak ammonias that condensation is got off are delivered to deammoniation tower (1) rectifying section top through weak ammonia reflux pump (14), flow from top to bottom after cloth liquid, contact with the secondary steam risen from stripping section is reverse, major part ammonia is overflowed from weak ammonia, transfer in secondary steam, when arriving stripping section top liquid distributor, ammonia level wherein reaches balance with ammonia level in the remained ammonia entering deammoniation tower (1) stripping section top, carries out deamination through stripping section downwards together after the two mixing;
The noncondensable gas be not condensed of condenser (6) shell side is constantly extracted out by vacuum pump (7); Vacuum pump (7) and the direct UNICOM of ammonia absorber (8) hypomere, the ammonia gas mixture of extraction introduces ammonia absorber (8) hypomere first order absorption pars infrasegmentalis by vacuum pump;
D, ammonia absorber (8) point two sections: hypomere is first order absorption section, and epimere is secondary absorber portion, adopt de-salted water to absorb; According to ammonia level in remained ammonia and the concentration requirement reclaiming ammoniacal liquor, by de-salted water spray pump, de-salted water is quantitatively transferred to ammonia absorber (8) top, secondary absorber portion packing layer upper strata is evenly sprayed onto by nozzle, flow through secondary absorber portion packing layer from top to bottom, secondary absorption is carried out to unabsorbed ammonia after first order absorption section absorbs; De-salted water becomes weak ammonia after absorbing ammonia, continues to be downward through first order absorption section packing layer, carries out first order absorption to the ammonia gas mixture introduced from ammonia absorber (8) bottom; In absorption process, weak ammonia concentration improves constantly;
Consider in ammonia absorption process and discharge a large amount of heats, ammonia absorber (8) height is set up, weak ammonia and the part ammonia of bottom, absorption tower (8) flow out naturally from tower base cone body mouth, enter ammoniacal liquor water cooler (10), the recirculated cooling water of cooled device shell side is cooled to 35-40 DEG C indirectly, along with temperature reduces, ammonia is absorbed further by weak ammonia, and then gravity flow enters weak ammonia tank (11);
Concentration requirement is not reached for preventing a cyclic absorption ammonia concn, first order absorption circulated sprinkling pump (9) is set, weak ammonia is delivered to ammonia absorber (8) first order absorption section top from weak ammonia tank (11), first order absorption section packing layer upper strata is evenly sprayed onto by nozzle, together with the weak ammonia that secondary absorber portion flows down, as the absorption liquid of first order absorption section, cyclic absorption is carried out to the ammonia gas mixture passed by bottom, absorption tower from top to bottom;
When weak ammonia tank (11) ammonia concn reaches requirement, be delivered to by qualified aqua ammonia pump (12) that strong aqua storage tank (13) is for subsequent use or standby to be sold.
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| CN105481036A (en) * | 2015-11-06 | 2016-04-13 | 王文领 | Energy-saving type negative-pressure deamination method of coked residual ammonia water |
| CN106219644A (en) * | 2016-08-15 | 2016-12-14 | 扬州晨化新材料股份有限公司 | Ammonia, Water Sproading the method preparing ammonia in a kind of polyetheramine production process |
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| CN112499710A (en) * | 2020-10-20 | 2021-03-16 | 阮氏化工（常熟）有限公司 | Device and method for purifying ammonia water by using ammonia-containing wastewater |
| CN114642895A (en) * | 2020-12-18 | 2022-06-21 | 陕西青朗万城环保科技有限公司 | High concentration ammonia treatment facility |
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| CN114516701A (en) * | 2022-03-15 | 2022-05-20 | 深圳市盛源环境科技有限公司 | Method and device for treating ammonia-containing wastewater |
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