CN102503011A - Method and device for thermally separating high-concentration ammonia nitrogen waste water - Google Patents
Method and device for thermally separating high-concentration ammonia nitrogen waste water Download PDFInfo
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- CN102503011A CN102503011A CN2011103447441A CN201110344744A CN102503011A CN 102503011 A CN102503011 A CN 102503011A CN 2011103447441 A CN2011103447441 A CN 2011103447441A CN 201110344744 A CN201110344744 A CN 201110344744A CN 102503011 A CN102503011 A CN 102503011A
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Abstract
The invention discloses a method for separating high-concentration ammonia nitrogen waste water by thermally promoting multi-effect flash evaporation-concentration-condensation-liquid film rectification. High-concentration ammonia nitrogen waste water is purified into condensed water of which the ammonia nitrogen concentration is lower than 20 mg/L by using low-position heat energy of which the temperature is 45-100 DEG C, particularly waste heat, and over 98 percent of ammonia nitrogen substances in waste water are enriched into a residual concentrated solution of which the volume is reduced by over 90 percent to obtain an organic liquid fertilizer and a recyclable nitrogen-enriched zymotic fluid, so that pollutant treatment and circular utilization are realized from a source. A device applied to the method is characterized in that: flash evaporators of various effects are arranged at different heights, so that the concentrated solution automatically flows towards equipment required by a process in an overflow way from the start of a final effect to an initial effect; condensation-heat exchange devices of various effects are arranged at different heights, so that all condensed water automatically flows towards a liquid sealing groove, and liquid is not left at positions over the condensed water outlet of each condensation-heat exchange device; and a hydraulic ejector is used for sucking ammonia-containing non-condensable gases in each piece of equipment of the device, and forced circulation is constituted, so that two-phase flow heat transfer of an absorption pipe is promoted, and absorption heat is dissipated to an environment.
Description
Technical field
The present invention relates to high-concentration ammonia nitrogenous wastewater and handle and the recycle utilization field, particularly utilize low grade heat energy high-concentration ammonia nitrogenous wastewater to be carried out the method and the process system of heating power isolation of purified.
Background technology
The ammonia nitrogen waste water that a lot of occasions such as industry, aquaculture and city refuse landfill produce, its ammonia nitrogen concentration is up to thousands of even tens thousand of mg/L.Prior art adopts the treatment process of air stripping → bio-transformation → chemical purification → qualified discharge more, increased topsoil and water surrounding load, and long processing period, working cost is high.Above-mentioned on the other hand occasion often will be discharged low level used heat, not only expended energy but also cause thermal pollution.Separate if rationally utilize low level used heat that high-concentration ammonia nitrogenous wastewater is carried out heating power, it is purified be the water of condensation recycle, but ammonia nitrogen then enrichment become organic fertilizer to remaining liquid concentrator.But prior art can't realize the sepn process of this high-concentration ammonia nitrogenous wastewater heating power.
Summary of the invention
The present invention discloses a kind of method; Through the multi-effect flashing steam degassing, spray the heating power tripping device of process such as absorptions, multiple-effect evaporation-condensation, liquid film rectifying and equipment formation; Make high-concentration ammonia nitrogenous wastewater be cleaned the water of condensation that is lower than 20mg/L for ammonia nitrogen concentration, and make the enrichment of ammonia nitrogen material in remaining liquid concentrator, become organic fertilizer.
The present invention mainly invents thought: heating power promotes high-concentration ammonia nitrogenous wastewater generation multi-effect flashing steam and is separated into gas-liquid two-phase; The ammonia that flashes off-water binary mixed vapour separates into the gas phase that ammonia nitrogen concentration is lower than water of condensation and the rich ammonia of 20mg/L through the liquid film rectifying; Because of the spissated raffinate of flash distillation becomes organic fertilizer through the gas of cooling and the rich ammonia of reduction pH value post-absorption, realize that thus the heating power of high-concentration ammonia nitrogenous wastewater separates.
Technical essential of the present invention is: utilizing temperature is that 45 ℃～100 ℃ heating agent provides heat energy for just imitating flash separation; After just the effect ammonia nitrogen waste water is heated to the temperature than low 5 ℃～10 ℃ of heating agent by partition; Under the vapor liquid equilibrium pressure suitable, carry out ammonia nitrogen waste water flash distillation-concentrate just imitating flashing chamber with this temperature; Liquid concentrator flows into the dope groove than the low at least 9m in riser position automatically from riser; The ammonia that flashes off-water binary mixed vapour is then at first generation filmwise condensation of prolong outer side surface and liquid film rectifying heat and mass of imitating shell-and-tube condensation-interchanger; Make the water of condensation ammonia nitrogen concentration be lower than 20mg/L and flow into the water of condensation liquid seal trough automatically; And uncooled ammonia enriched gas is lower than 40 ℃, pH value through valve, gas phase pipe and hydraulic ejector by temperature and is no more than 8.0 first effect liquid concentrator suction, thus ammonia nitrogen waste water is separated into the water of condensation that conforms with environmental requirement and the liquid concentrator of rich nitrogen.Ammonia-water binary mixed vapour condensation the latent heat of just imitating is used for heating mobile one in first effect shell-and-tube condensation-Tube Sheet of Heat Exchanger and imitates ammonia nitrogen waste water; Making it under lower temperature (just imitating 5 ℃～10 ℃ of ammonia-water binary mixed vapour condensation temperature such as being lower than) imitates in the flasher and one imitates and carry out flash distillation-concentrate and ammonia-water binary mixed vapour condensation and liquid film rectifying in shell-and-tube condensation-interchanger one; Imitating ammonia nitrogen waste water with one is separated into one and imitates liquid concentrator, ammonia nitrogen concentration and be lower than one of the 20mg/L gas phase of ammonia nitrogen of having imitated water of condensation and enrichment; One imitates liquid concentrator carries out the sepn process of aforesaid effect just from the first effect flashing chamber that an effect flasher riser flows into than low 2 ~ 6 m in riser position automatically under the hydrostatic column effect; One imitates rich ammonia gas is also aspirated by the aforesaid liquid concentrator of just imitating; One imitates water of condensation flows into same low level liquid seal trough automatically with the first water of condensation of imitating, and the riding position of this liquid seal trough is than the low at least 9m of condensation-water drain of all condensation-interchanger in this device.One imitates flash distillation binary mixed vapour condensation latent heat is used for heating mobile two effect ammonia nitrogen waste waters in an effect shell-and-tube condensation-Tube Sheet of Heat Exchanger; Make it in than two effect flashers of low 5 ℃～10 ℃ of an effect binary mixed vapour condensation temperature with in two effect shell-and-tube condensation-interchanger, to carry out flash distillation-concentrated and ammonia-water binary mixed vapour condensation and liquid film rectifying; Imitating ammonia nitrogen waste waters with two again is separated into two and imitates liquid concentrators, ammonia nitrogen concentration and be lower than two of 20mg/L and imitate water of condensation and rich ammonia mutually; Two effect liquid concentrators are imitated flasher risers automatic effect flashing chamber that flows under the hydrostatic column effect from two and are carried out an aforesaid effect sepn process; Two imitate rich ammonia gas by just imitating the liquid concentrator suction as stated, and two effect water of condensation get into same low level liquid seal trough and collect.Aforesaid one imitates with two effect processes and equipment basic identically, and different is two imitates fluid temperatures and imitate low 5 ℃～10 ℃ of liquid, two than one and imitate the flasher riding positions and imitate high 2 ~ 6 m of flasher to guarantee that two imitate liquid concentrators automatic inflow one effect flashing chamber under the hydrostatic column effect than one.By and one imitate and two imitate same flow process and method, the treatment unit that (2+n) imitates can be set, that is: this device comprises at least just imitating with the end and imitates, to the restricted condition of n be in the last effect flasher vapor liquid equilibrium temperature than at least 10 ℃ of envrionment temperature height.The alkaline assistant that will add that the primary high-concentration ammonia nitrogenous wastewater gets into before imitate at the end makes its pH value be higher than 9.0; Preheating temperature is higher than 45 ℃; The boiling degassing in degas chamber; Ammoniated noncondensable gas is gone through the hydraulic ejector suction by the aforesaid liquid concentrator of just imitating, and adds acid additive readjustment ammonia nitrogen waste water pH value after the degassing again to being no more than 8.0, and the entering end is imitated and separated then.
Usefulness of the present invention is to utilize 45 ℃～100 ℃ Lowlevel thermal energy, especially used heat; High-concentration ammonia nitrogenous wastewater is purified the water of condensation that is lower than 20mg/L for ammonia nitrogen concentration through flash distillation-concentrate with liquid film rectifying; And make ammonia nitrogen material enrichment more than 98% become the fermented liquid of organic fertilizer or reusable edible in the remaining liquid concentrator, thereby realize pollutant control and recycle in the source.The present invention efficiently utilizes Lowlevel thermal energy, 2600 * 10
3KJ heat energy can be handled (2+n) ton waste water.
Description of drawings
Accompanying drawing is the device synoptic diagram that 3 of n=1 provided by the invention is imitated heating power separation of high-concentration ammonia nitrogen waste water.Among the figure: the 1-preheater; The 2-condensate draining; 3-adds the alkali groove; The 4-degassing vessel; The 5-hydraulic ejector; The 6-concentrate pump; 7-dope groove; 8-is imitated pump in the end; 9-one is imitated condensation-interchanger; 10-is imitated flasher in the end; 11-one is imitated pump; 12-is just imitated condensation-interchanger; 13-one is imitated flasher; 14-is just imitated pump; 15-is just imitated well heater; 16-is just imitated flasher; The former water heater of 17-; 18-gas phase pipe; 19-is just imitated the liquid concentrator pipe.Below in conjunction with embodiment accompanying drawing is done further to set forth.
Embodiment
Below in conjunction with but be not limited to embodiment and set forth the specific embodiment of the invention
Embodiment 1: plant's natural pond liquid, more than the ammonia nitrogen concentration 3000mg/L, use 75 ℃～95 ℃ hot water to be separated into the water of condensation and the organic fertilizer that concentrates more than 10 times that ammonia nitrogen concentration is lower than 20mg/L as heating agent.
Adopt shown in the drawings 3 to imitate heating power separation of high-concentration ammonia nitrogen waste water device.Just imitating pump 14 makes the first ammonia nitrogen waste water of imitating imitate well heater 15 and just imitate circulation between the flasher 16 first; With 75 ℃～95 ℃ circulating hot waters is that heating agent is kept just 70 ℃～90 ℃ of flash vaporization points of effect, flashing pressure 31 ~ 70 kPa (cutting off); The ammonia that flashes off-water binary mixed vapour carries out liquid film rectifying heat and mass transfer process simultaneously in the prolong outer side surface filmwise condensation of effect condensation-interchanger 12 just; Make ammonia be enriched in gas phase and pass through valve and get into gas phase pipe 18 by hydraulic ejector 5 suctions; Ammonia nitrogen concentration is lower than the automatic inflow of water of condensation of 20mg/L and the condensate draining 2 of atmosphere; First effect liquid concentrator automatic overflow is gone into the dope groove 7 with atmosphere; Getting into hydraulic ejectors 5 suctions through concentrate pump 6 pressurization contains ammonia phase material and constitutes pump circulation and impel the absorption tube two to conduct heat to distribute to environment and absorb heat and make liquid concentrator keep temperature to be lower than 40 ℃; Replenish acidic medium to the dope groove simultaneously and make pH value be no more than 8.0, absorbing enriched the liquid concentrator of ammonia nitrogen export as the organic fertilizer product, water of condensation then returns plant and recycles.One effect pump 11 makes in the Tube Sheet of Heat Exchanger of an effect ammonia nitrogen waste water through first effect condensation-interchanger 12 and is heated to 60 ℃～80 ℃; Get into one and imitate flasher 13 flash concentration; Flashing pressure 20 ~ 48 kPa (cutting off); The liquid concentrator automatic overflow goes into just to imitate flasher 16; The ammonia that flashes off-water binary mixed vapour carries out liquid film rectifying simultaneously in the prolong outer side surface filmwise condensation of an effect condensation-interchanger 9, and ammonia is enriched in gas phase and through being aspirated by hydraulic ejector 5 valve and gas phase pipe 18, the effect water of condensation that ammonia nitrogen concentration is lower than 20mg/L flows into condensate draining 2 automatically.End effect pump 8 circulates the last ammonia nitrogen waste water of imitating in the Tube Sheet of Heat Exchanger of an effect condensation-interchanger 9 and between the effect flasher 10 of end; Utilize an effect flash distillation mixed vapour condensation latent heat to keep the end and imitate 50 ℃～70 ℃ of flash vaporization points, flashing pressure 12 ~ 31 kPa (cutting off); End effect liquid concentrator automatic overflow is gone into an effect flasher 13; The ammonia that flashes off-water binary mixed vapour carries out liquid film rectifying simultaneously in the prolong outer side surface filmwise condensation of former water heater 17; Rich ammonia gas is aspirated by hydraulic ejector 5 through the gentle continuous siphunculus 18 of valve, and the water of condensation that ammonia nitrogen concentration is lower than 20mg/L flows into condensate draining 2 automatically.Natural pond liquid waste water is warmed up to more than 45 ℃, makes the pH value be higher than 9.0, in degassing vessel 4, aspirated the degassing of seething with excitement by hydraulic ejector 5 then through adding alkali groove 3 interpolation alkaline assistants 1 again through preheater 1 earlier before getting into last effect; Add acid additive after the degassing again and adjust back to ammonia nitrogen waste water pH value and be no more than 8.0, get into the end and imitate flasher 10.
This routine result of implementation makes plant's natural pond liquid of 1 ton of ammonia nitrogen concentration 3000mg/L be separated into about 0.9 ton of ammonia nitrogen concentration with 10 tons 75 ℃～95 ℃ hot water circulation and is lower than the water of condensation of 20mg/L and the organic fertilizer that about 0.1 ton of ammonia nitrogen concentration is higher than 30000mg/L.
Embodiment 2: the city refuse landfill percolate more than the ammonia nitrogen concentration 2000mg/L, is separated into the water of condensation and the liquid that recharges that concentrates more than 10 times that ammonia nitrogen concentration is lower than 20mg/L with 75 ℃～95 ℃ hot water circulation.
Adopt shown in the drawings 3 to imitate heating power separation of high-concentration ammonia nitrogen waste water devices and the process method identical, make the percolate of 1 ton of ammonia nitrogen concentration 2000mg/L be separated into about 0.9 ton of ammonia nitrogen concentration with 10 tons 75 ℃～95 ℃ hot water circulation and be lower than the water of condensation of 20mg/L and the liquid that recharges that about 0.1 ton of ammonia nitrogen concentration is higher than 20000mg/L with embodiment 1.The effect of present embodiment is with returning the refuse landfill sealing treatment after the separated from contaminants in the percolate.
Claims (2)
1. a heating power promotes the method for high-concentration ammonia nitrogenous wastewater multi-effect flashing steam-concentrate and liquid film rectifying; It is characterized in that making the ammonia-water binary mixed vapour that flashes off through filmwise condensation and liquid film rectifying; Spray the uncooled ammonia enriched gas of absorption with liquid concentrator; Make that the ammonia nitrogen material more than 98% is absorbed by liquid concentrator in the waste water, the ammonia nitrogen concentration of water of condensation is lower than 20mg/L; Utilize 45 ℃～100 ℃ Lowlevel thermal energy to promote just to imitate flash distillation-concentrated-sepn process; The mixed vapour condensation latent heat of just imitating flash distillation is used to promote one and imitates flash distillation-concentrated-sepn process; One imitates flash vaporization point than low 5 ℃～10 ℃ of the mixed vapour condensation temperature of just imitating flash distillation; The mixed vapour condensation latent heat of one effect flash distillation is imitated flash distillations-concentrated-sepn processes by same principle promotion two again, and formation multiple-effect that the rest may be inferred by analogy is separated until end effect flash vaporization point higher 10 ℃ than envrionment temperature at least; To be preheating to temperature before primary high-concentration ammonia nitrogenous wastewater entering end effect flash distillation-concentrate-separation and be higher than 45 ℃; Adding alkaline assistant makes its pH value be higher than 9.0; The boiling degassing in degas chamber; Ammoniated noncondensable gas is gone through the hydraulic ejector suction by liquid concentrator, and the ammonia nitrogen waste water after the degassing adds acid additive and returns adjust pH to being no more than 8.0; Be used to spray the liquid concentrator that suction contains the ammonia noncondensable gas and keep temperature to be lower than 40 ℃, the pH value is no more than 8.0.
2. one kind is used for heating power promotion high-concentration ammonia nitrogenous wastewater multi-effect flashing steam-concentrated-isolating device; It is characterized in that with containing the ammonia noncondensable gas in the individual device of this device of waterpower sprayer pumps, and constitute pump circulation and impel the absorption tube two to conduct heat to distribute and absorb heat to environment; Each is imitated the flasher discrepancy in elevation and arranges, guarantees to imitate beginning up to first effect from the end, and liquid concentrator is all with the equipment of overflow mode automatic stream processing requirement; Each is imitated the condensation-interchanger discrepancy in elevation and arranges, guarantees the equal automatic stream liquid seal trough of whole water of condensation, and the condensation-water drain that guarantees each condensation-interchanger is with upper part retain liquid not.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011103447441A CN102503011A (en) | 2011-11-04 | 2011-11-04 | Method and device for thermally separating high-concentration ammonia nitrogen waste water |
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| CN2011103447441A CN102503011A (en) | 2011-11-04 | 2011-11-04 | Method and device for thermally separating high-concentration ammonia nitrogen waste water |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107162305A (en) * | 2017-07-07 | 2017-09-15 | 金川集团股份有限公司 | A kind of acid waste water processing unit and its application method |
| CN110835136A (en) * | 2019-12-12 | 2020-02-25 | 江苏新河农用化工有限公司 | Ammonia nitrogen wastewater treatment system and method |
| CN114031235A (en) * | 2021-11-26 | 2022-02-11 | 江苏理文化工有限公司 | Method for recovering nitrogen-containing wastewater |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1935677A (en) * | 2006-10-20 | 2007-03-28 | 太原海力丰科技发展有限公司 | Ammonium nitrate waste water treatment method |
| CN101913669A (en) * | 2010-09-06 | 2010-12-15 | 济南冶金化工设备有限公司 | Multi-effect energy-saving ammonia recovery process and device |
| CN102020327A (en) * | 2010-09-21 | 2011-04-20 | 广州市心德实业有限公司 | Ammonia nitrogen waste water treatment equipment |
-
2011
- 2011-11-04 CN CN2011103447441A patent/CN102503011A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1935677A (en) * | 2006-10-20 | 2007-03-28 | 太原海力丰科技发展有限公司 | Ammonium nitrate waste water treatment method |
| CN101913669A (en) * | 2010-09-06 | 2010-12-15 | 济南冶金化工设备有限公司 | Multi-effect energy-saving ammonia recovery process and device |
| CN102020327A (en) * | 2010-09-21 | 2011-04-20 | 广州市心德实业有限公司 | Ammonia nitrogen waste water treatment equipment |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107162305A (en) * | 2017-07-07 | 2017-09-15 | 金川集团股份有限公司 | A kind of acid waste water processing unit and its application method |
| CN110835136A (en) * | 2019-12-12 | 2020-02-25 | 江苏新河农用化工有限公司 | Ammonia nitrogen wastewater treatment system and method |
| CN114031235A (en) * | 2021-11-26 | 2022-02-11 | 江苏理文化工有限公司 | Method for recovering nitrogen-containing wastewater |
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Application publication date: 20120620 |