CN107792904A - A kind of technique and device of continuous removal of ammonia and nitrogen light component organic matter and salt - Google Patents
A kind of technique and device of continuous removal of ammonia and nitrogen light component organic matter and salt Download PDFInfo
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- CN107792904A CN107792904A CN201711004867.4A CN201711004867A CN107792904A CN 107792904 A CN107792904 A CN 107792904A CN 201711004867 A CN201711004867 A CN 201711004867A CN 107792904 A CN107792904 A CN 107792904A
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- level
- evaporator
- tower reactor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
Abstract
The invention belongs to technical field of waste water processing, is specifically related to a kind of continuous removal of ammonia and nitrogen light component organic matter and salt technique and system.A kind of waste water ammonia-removal nitrogen desalination process, it is characterised in that comprise the following steps that：Step 1：Rectifying tower reactor is distilled；Step 2：One-level is evaporated；Step 3：Dual evaporation；... step n：N levels are evaporated：Step n+1：Whole level evaporation.Change system used in a kind of waste water ammonia-removal nitrogen desalinating process, including rectifying tower reactor, one-level evaporator, dual evaporation tank and n level evaporators.Beneficial effects of the present invention：1) the light component organic matter in waste water, especially ammoniacal liquor are reclaimed, and purity is high；2) salt in final waste water is eventually converted into solid powder, reduces solid waste discharge；3) take off gently and take off and couple again, reduce plant running energy consumption 40%~70%；4) for waste water after de- light and desalination, obtaining clean water can be used as process water return system to recycle, and reduce the consumption of water.
Description
Technical field
The invention belongs to technical field of waste water processing, a kind of waste water ammonia-removal nitrogen desalination process and used is specifically related to
Change system.
Background technology
Industrial wastewater is industrial pollutants common in chemical process, if the life that directly discharge will be to us
Environment produces destruction, our health of serious threat.And common one kind alkalescence containing NH4 wastewater from chemical industry, optimization can be passed through
Processing reduces its pollution to environment, and processing of traditional handling process to the wastewater from chemical industry of alkalescence containing NH4 be not thorough, processing production
Thing is not pure, it is impossible to reaches the purpose for realizing twice laid.
The content of the invention
The present invention makes up the deficiency of conventional art to solve problem mentioned above, there is provided one kind processing is efficient, thorough
Bottom, production safety, highly reliable waste water ammonia-removal nitrogen desalination process and change system used.
The present invention is achieved through the following technical solutions：
A kind of technique of continuous removal of ammonia and nitrogen light component organic matter and salt, it is characterised in that comprise the following steps that：
Step 1：Rectifying tower reactor is distilled：By the waste water outside battery limit (BL), heated by preheater, be then sent to rectifying
Rectification process is carried out in tower reactor, after ammonia steam introduces condenser condensation process by the tower top of rectifying tower reactor, then is evaporated via tower reactor
Tank evaporates, and distinguishing branch by tower reactor reflux pump is pressed into ammonia outlet and rectifying tower reactor top rectifying circular treatment again；Rectifying
Aqueous slkali is also added by the external world in the distillation process of tower reactor；The bottom liquid of rectifying tower reactor is pressed into rectifying tower reactor by tower reactor reboiler
It is interior, circulate rectification process；
Step 2：One-level is evaporated：The waste water that will be flowed out after rectifying tower reactor rectifying, one-level is pumped into by tower reactor extraction and evaporated
Processing is evaporated in tank, steam is entered in rectifying tower reactor by tower reactor reboiler, again rectification process；The bottom liquid of one-level evaporator
Entered by one-level evaporator in one-level evaporator, circulating and evaporating processing；
Step 3：Dual evaporation：The waste water flowed out after one-level evaporator is evaporated, two level is pressed into by one-level transfering material pump and steamed
Send out and re-evaporation processing is carried out in tank, steam is entered in one-level evaporator by one-level evaporator, again evaporation process；Dual evaporation tank
Bottom liquid by secondary evaporimeter enter dual evaporation tank in, circulating and evaporating processing；
……
Step n：N levels are evaporated：The waste water flowed out after n-1 levels evaporator is evaporated, n levels are pressed into by n-1 levels transfering material pump and steamed
Send out and re-evaporation processing is carried out in tank, steam is entered in n-1 level evaporators by n-1 levels evaporator, again evaporation process；N levels are evaporated
The bottom liquid of tank is entered in n level evaporators by n levels evaporator, circulating and evaporating processing；
Step n+1：Whole level evaporation：The waste water flowed out after n levels evaporator is evaporated, whole level is pressed into by n levels transfering material pump and steamed
Send out and re-evaporation processing is carried out in tank, steam is entered in n level evaporators by n levels evaporator, again evaporation process；Whole level evaporator
Bottom liquid is entered in whole level evaporator by whole level evaporator, and pressure, circulating and evaporating processing are provided by circulating pump；Whole level evaporator
Bottom liquid is introduced in drier and picked out after drying process by solid salt outlet；Another whole level evaporator provides saturated steam by the external world；
The natural number that n in step n and step n+1 described above is 1,2,3.......
It is described by the waste water outside battery limit (BL), be heated to 95 DEG C by preheater.
The tower top temperature of described rectifying tower reactor ensures that overhead extraction ammonia concn is 9~15%, cold at 95~100 DEG C
But temperature is 35~40 DEG C after.
The steam pressure of described one-level evaporator outflow be P=0.1MPa, T=122 DEG C of vapor (steam) temperature, what bottom was flowed out
Brine waste temperature T≤125 DEG C.
The steam pressure of described dual evaporation tank outflow is P=0.25MPa), T=138.8 DEG C of vapor (steam) temperature, bottom stream
Brine waste temperature T≤125 DEG C gone out.
The steam pressure of described three-level evaporator outflow is P=0.4MPa), T=151.7 DEG C of vapor (steam) temperature.
The whole level evaporation pot bottom extraction be full of or oversaturated salting liquid is delivered to centrifugation, press filtration work by pump
The water of section or drying machine evaporation drying, press filtration or evaporation removes waste water head tank, obtains containing salt solid powder.
A kind of system of continuous removal of ammonia and nitrogen light component organic matter and salt, including rectifying tower reactor, one-level evaporator, two level are steamed
Send out tank and n level evaporators, it is characterised in that：The one-level preheater of waste water heat effect is connected on the top of rectifying tower reactor by pipeline
With raw material two level preheater, the top of rectifying tower reactor connects condenser by conduit and enters port, condenser exit port connection tower reactor
Evaporator, tower reactor evaporator connect the top of rectifying tower reactor by tower reactor backflow catheter pump, and the bottom of rectifying tower reactor passes through tower reactor
Reboiler circulates bottom liquid to rectifying tower reactor；Rectifying tower reactor is provided with the interface for accessing extraneous aqueous slkali；
The bottom of rectifying tower reactor produces pump pipeline communication one-level evaporator by tower reactor, and the bottom of one-level evaporator passes through one
Level evaporator circulates bottom liquid to one-level evaporator；
By one-level transfering material pump pipeline communication dual evaporation tank, the bottom of dual evaporation tank passes through for the bottom of one-level evaporator
Secondary evaporimeter circulates bottom liquid to dual evaporation tank；
By two level transfering material pump pipeline communication n level evaporators, the bottom of n level evaporators passes through n for the bottom of dual evaporation tank
Level evaporator circulates bottom liquid to n level evaporators；
The bottom of n level evaporators is connected by n level transfering material pump pipeline communication end level evaporators, the lower pipeline of whole level evaporator
Circulating pump is connect, circulating pump pipeline connects whole level evaporator, and whole level evaporator pipeline connects whole level evaporator；The bottom of whole level evaporator
Portion's pipeline communication drier；Whole level evaporator pipeline is additionally provided with the extraneous saturated steam interface of access.
The whole level evaporator pipeline connection raw material one-level preheater of described one-level evaporator, secondary evaporimeter ...
Described whole level evaporator pipeline connection raw material two level preheater.
Beneficial effects of the present invention：1) the light component organic matter in waste water, especially ammoniacal liquor are reclaimed, and purity is high；2) most
Salt in whole waste water is eventually converted into solid powder, reduces solid waste discharge；3) take off gently and take off and couple again, reduce plant running energy
Consumption 40%~70%；4) for waste water after de- light and desalination, obtaining clean water can be used as the circulation of process water return system to make
With reducing the consumption of water.
Brief description of the drawings
The present invention is further illustrated below in conjunction with the accompanying drawings.
Fig. 1 is present system structural representation；
In figure, the outlet of 1 steam condensation water, 2 waste water material inlets, 3 temperaturing control pressure valves, 4 raw material one-level preheaters, 5 raw materials two
Level preheater, 6 rectifying tower reactors, 7 condensers, 8 tower reactor evaporators, 9 tower reactor reflux pumps, 10 tower reactor reboilers, 11 tower reactors extraction pump,
12 one-level evaporators, 12-1 one-level evaporators, 12-2 one-level transfering material pumps, 13 dual evaporation tanks, 13-1 secondary evaporimeters, 13-2 bis-
Level transfering material pump, 14 three-level evaporators, 14-1 three-level evaporators, 14-2 circulating pumps, 15 driers, 16 aqueous slkali imports, 17 ammonias
Outlet, 18 saturated steams, the outlet of 19 solid salts, 20 fluid level control valves.
Embodiment
Accompanying drawing is a kind of specific embodiment of the invention.
The technique of continuous the removal of ammonia and nitrogen light component organic matter and salt of the present invention, is comprised the following steps that：
Step 1：Rectifying tower reactor is distilled：By the waste water outside battery limit (BL), heated by preheater, be then sent to rectifying
Rectification process is carried out in tower reactor, after ammonia steam introduces condenser condensation process by the tower top of rectifying tower reactor, then is evaporated via tower reactor
Tank evaporates, and distinguishing branch by tower reactor reflux pump is pressed into ammonia outlet and rectifying tower reactor top rectifying circular treatment again；Rectifying
Aqueous slkali is also added by the external world in the distillation process of tower reactor；The bottom liquid of rectifying tower reactor is pressed into rectifying tower reactor by tower reactor reboiler
It is interior, circulate rectification process；
Step 2：One-level is evaporated：The waste water that will be flowed out after rectifying tower reactor rectifying, one-level is pumped into by tower reactor extraction and evaporated
Processing is evaporated in tank, steam is entered in rectifying tower reactor by tower reactor reboiler, again rectification process；The bottom liquid of one-level evaporator
Entered by one-level evaporator in one-level evaporator, circulating and evaporating processing；
Step 3：Dual evaporation：The waste water flowed out after one-level evaporator is evaporated, two level is pressed into by one-level transfering material pump and steamed
Send out and re-evaporation processing is carried out in tank, steam is entered in one-level evaporator by one-level evaporator, again evaporation process；Dual evaporation tank
Bottom liquid by secondary evaporimeter enter dual evaporation tank in, circulating and evaporating processing；
Step 4：Whole level evaporation：The waste water flowed out after dual evaporation tank is evaporated, whole level is pressed into by two level transfering material pump and steamed
Send out and re-evaporation processing is carried out in tank, steam is entered in dual evaporation tank by secondary evaporimeter, again evaporation process；Whole level evaporator
Bottom liquid entered by whole level evaporator in whole level evaporator, provide pressure by circulating pump, circulating and evaporating processing；Whole level evaporator
Bottom liquid introduce in drier and picked out after drying process by solid salt outlet；Another whole level evaporator provides saturation water by the external world and steamed
Gas；
It is described by the waste water outside battery limit (BL), be heated to 95 DEG C by preheater.
The tower top temperature of described rectifying tower reactor ensures that overhead extraction ammonia concn is 9~15%, cold at 95~100 DEG C
But temperature is 35~40 DEG C after.
The steam pressure of described one-level evaporator outflow be P=0.1MPa, T=122 DEG C of vapor (steam) temperature, what bottom was flowed out
Brine waste temperature T≤125 DEG C.
The steam pressure of described dual evaporation tank outflow is P=0.25MPa), T=138.8 DEG C of vapor (steam) temperature, bottom stream
Brine waste temperature T≤125 DEG C gone out.
The steam pressure of described three-level evaporator outflow is P=0.4MPa), T=151.7 DEG C of vapor (steam) temperature.
The whole level evaporation pot bottom extraction be full of or oversaturated salting liquid is delivered to centrifugation, press filtration work by pump
The water of section or drying machine evaporation drying, press filtration or evaporation removes waste water head tank, obtains containing salt solid powder.
A kind of system of continuous removal of ammonia and nitrogen light component organic matter and salt, including rectifying tower reactor, one-level evaporator, two level are steamed
Tank and whole level evaporator are sent out, the top of rectifying tower reactor connects the one-level preheater and raw material two level of waste water heat effect by pipeline
Preheater, the top of rectifying tower reactor connect condenser by conduit and enter port, condenser exit port connection tower reactor evaporator, tower reactor
Evaporator connects the top of rectifying tower reactor by tower reactor backflow catheter pump, and bottom is circulated in the bottom of rectifying tower reactor by tower reactor reboiler
Liquid is to rectifying tower reactor；Rectifying tower reactor is provided with the interface for accessing extraneous aqueous slkali；
The bottom of rectifying tower reactor produces pump pipeline communication one-level evaporator by tower reactor, and the bottom of one-level evaporator passes through one
Level evaporator circulates bottom liquid to one-level evaporator；
By one-level transfering material pump pipeline communication dual evaporation tank, the bottom of dual evaporation tank passes through for the bottom of one-level evaporator
Secondary evaporimeter circulates bottom liquid to dual evaporation tank；
The bottom of dual evaporation tank passes through two level transfering material pump pipeline communication end level evaporator, the lower pipeline of whole level evaporator
Circulating pump is connected, circulating pump pipeline connects whole level evaporator, and whole level evaporator pipeline connects whole level evaporator；Whole level evaporator
Bottom pipe connects drier；Whole level evaporator pipeline is additionally provided with the extraneous saturated steam interface of access.Described one-level
The whole level evaporator pipeline connection raw material one-level preheater of evaporator, secondary evaporimeter ....Described whole level evaporator pipeline connection
Raw material two level preheater.
The general principle and principal character and advantages of the present invention of the present invention has been shown and described above.Above-described embodiment and
Merely illustrating the principles of the invention described in specification, without departing from the spirit and scope of the present invention, the present invention is also
Various changes and modifications are had, these changes and improvements all fall within the protetion scope of the claimed invention.It is claimed
Scope is by appended claims and its equivalent thereof.
Claims (10)
1. the technique of a kind of continuous removal of ammonia and nitrogen light component organic matter and salt, it is characterised in that comprise the following steps that：
Step 1：Rectifying tower reactor is distilled：By the waste water outside battery limit (BL), heated by preheater, be then sent to rectifying tower reactor
Interior carry out rectification process, after ammonia steam introduces condenser condensation process by the tower top of rectifying tower reactor, then via the steaming of tower reactor evaporator
Hair, branch is distinguished by tower reactor reflux pump and is pressed into ammonia outlet and rectifying tower reactor top rectifying circular treatment again；Rectifying tower reactor
Distillation process in also pass through and extraneous add aqueous slkali；The bottom liquid of rectifying tower reactor is pressed into rectifying tower reactor by tower reactor reboiler,
Circulate rectification process；
Step 2：One-level is evaporated：The waste water that will be flowed out after rectifying tower reactor rectifying, it is pumped into by tower reactor extraction in one-level evaporator
Processing is evaporated, steam is entered in rectifying tower reactor by tower reactor reboiler, again rectification process；The bottom liquid of one-level evaporator passes through
One-level evaporator enters in one-level evaporator, circulating and evaporating processing；
Step 3：Dual evaporation：The waste water flowed out after one-level evaporator is evaporated, dual evaporation tank is pressed into by one-level transfering material pump
Interior progress re-evaporation processing, steam are entered in one-level evaporator by one-level evaporator, again evaporation process；The bottom of dual evaporation tank
Liquid is entered in dual evaporation tank by secondary evaporimeter, circulating and evaporating processing；
……
Step n：N levels are evaporated：The waste water flowed out after n-1 levels evaporator is evaporated, n level evaporators are pressed into by n-1 levels transfering material pump
Interior progress re-evaporation processing, steam are entered in n-1 level evaporators by n-1 levels evaporator, again evaporation process；N level evaporators
Bottom liquid is entered in n level evaporators by n levels evaporator, circulating and evaporating processing；
Step n+1：Whole level evaporation：The waste water flowed out after n levels evaporator is evaporated, whole level evaporator is pressed into by n levels transfering material pump
Interior progress re-evaporation processing, steam are entered in n level evaporators by n levels evaporator, again evaporation process；The bottom liquid of whole level evaporator
Entered by whole level evaporator in whole level evaporator, pressure, circulating and evaporating processing are provided by circulating pump；The bottom liquid of whole level evaporator
Introduce in drier and picked out after drying process by solid salt outlet；Another whole level evaporator provides saturated steam by the external world；
The natural number that n in step n and step n+1 described above is 1,2,3.......
2. the technique of a kind of continuous removal of ammonia and nitrogen light component organic matter according to claim 1 and salt, it is characterised in that：Institute
State by the waste water outside battery limit (BL), be heated to 95 DEG C by preheater.
3. the technique of a kind of continuous removal of ammonia and nitrogen light component organic matter according to claim 1 and salt, it is characterised in that：Institute
The tower top temperature for the rectifying tower reactor stated ensures that overhead extraction ammonia concn is 9~15%, and temperature is after cooling at 95~100 DEG C
35~40 DEG C.
4. the technique of a kind of continuous removal of ammonia and nitrogen light component organic matter according to claim 1 and salt, it is characterised in that：Institute
The steam pressure for the one-level evaporator outflow stated be P=0.1MPa, T=122 DEG C of vapor (steam) temperature, the brine waste temperature that bottom is flowed out
Spend T≤125 DEG C.
5. the technique of a kind of continuous removal of ammonia and nitrogen light component organic matter according to claim 1 and salt, it is characterised in that：Institute
The steam pressure for the dual evaporation tank outflow stated is P=0.25MPa), T=138.8 DEG C of vapor (steam) temperature, the saliferous of bottom outflow gives up
Coolant-temperature gage T≤125 DEG C.
6. the technique of a kind of continuous removal of ammonia and nitrogen light component organic matter according to claim 1 and salt, it is characterised in that：Institute
The steam pressure for the three-level evaporator outflow stated is P=0.4MPa), T=151.7 DEG C of vapor (steam) temperature.
7. the technique of a kind of continuous removal of ammonia and nitrogen light component organic matter according to claim 1 and salt, it is characterised in that：Institute
State the evaporation pot bottom extraction of whole level be full of or oversaturated salting liquid is delivered to centrifugation, press filtration workshop section or drying machine by pump
The water of evaporation drying, press filtration or evaporation removes waste water head tank, obtains containing salt solid powder.
8. a kind of continuous removal of ammonia and nitrogen light component organic matter and salt system, including rectifying tower reactor, one-level evaporator, dual evaporation tank
With n level evaporators, it is characterised in that：The top of rectifying tower reactor connects the one-level preheater and original of waste water heat effect by pipeline
Expect two level preheater, the top of rectifying tower reactor connects condenser by conduit and enters port, the connection tower reactor evaporation of condenser exit port
Tank, tower reactor evaporator connect the top of rectifying tower reactor by tower reactor backflow catheter pump, and the bottom of rectifying tower reactor is boiled again by tower reactor
Device circulates bottom liquid to rectifying tower reactor；Rectifying tower reactor is provided with the interface for accessing extraneous aqueous slkali；
The bottom of rectifying tower reactor produces pump pipeline communication one-level evaporator by tower reactor, and the bottom of one-level evaporator is steamed by one-level
Send out device and circulate bottom liquid to one-level evaporator；
By one-level transfering material pump pipeline communication dual evaporation tank, the bottom of dual evaporation tank passes through two level for the bottom of one-level evaporator
Evaporator circulates bottom liquid to dual evaporation tank；
By two level transfering material pump pipeline communication n level evaporators, the bottom of n level evaporators is steamed by n levels for the bottom of dual evaporation tank
Send out device and circulate bottom liquid to n level evaporators；
The bottom of n level evaporators is followed by n level transfering material pump pipeline communication end level evaporators, the lower pipeline connection of whole level evaporator
Ring pump, circulating pump pipeline connect whole level evaporator, and whole level evaporator pipeline connects whole level evaporator；The lower tube of whole level evaporator
Road connects drier；Whole level evaporator pipeline is additionally provided with the extraneous saturated steam interface of access.
9. a kind of continuous removal of ammonia and nitrogen light component organic matter according to claim 8 and salt system, it is characterised in that：It is described
One-level evaporator, secondary evaporimeter ... whole level evaporator pipeline connection raw material one-level preheater.
10. a kind of continuous removal of ammonia and nitrogen light component organic matter according to claim 8 and salt system, it is characterised in that：Institute
The whole level evaporator pipeline connection raw material two level preheater stated.
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| CN201711004867.4A CN107792904A (en) | 2017-10-25 | 2017-10-25 | A kind of technique and device of continuous removal of ammonia and nitrogen light component organic matter and salt |
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| CN108341447A (en) * | 2018-04-04 | 2018-07-31 | 烟台国邦化工机械科技有限公司 | A kind of waste liquid continuously takes off light desalination process and system |
| CN108467076A (en) * | 2018-06-01 | 2018-08-31 | 烟台国邦化工机械科技有限公司 | Based on the process and device for strengthening resolving resourceization processing waste water containing low-boiling-point substance |
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