CN106007145A - Residual ammonia water treatment method and system - Google Patents
Residual ammonia water treatment method and system Download PDFInfo
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- CN106007145A CN106007145A CN201610522602.2A CN201610522602A CN106007145A CN 106007145 A CN106007145 A CN 106007145A CN 201610522602 A CN201610522602 A CN 201610522602A CN 106007145 A CN106007145 A CN 106007145A
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
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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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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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
- C02F1/048—Purification of waste water by evaporation
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- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- 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
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
- C02F2101/18—Cyanides
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
- C02F2101/345—Phenols
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
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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
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- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C—CHEMISTRY; METALLURGY
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- C02F2209/44—Time
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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Abstract
The invention discloses a residual ammonia water treatment method and system. The method includes the steps that residual ammonia water generated in the coking process is subjected to pretreatment of oil removal and suspended matter removal; the pretreated residual ammonia water is heated to set temperature; the residual ammonia water heated to the set temperature is injected into a first ammonia still for first steam gas stripping treatment; alkali liquor is added into the ammonia water obtained after first steam gas stripping treatment for pH value adjustment, the pH value of the ammonia water obtained after first steam gas stripping treatment is adjusted to a preset value, and the preset value is larger than or equal to 10; the ammonia water obtained after pH value adjustment is input in a second ammonia still for second steam gas stripping treatment, and the waste water obtained after ammonia distillation is obtained. According to the technical scheme, the technical problem that the use amount of the alkali liquor is too large during residual ammonia water treatment in the prior art is solved, the use amount of the alkali liquor is reduced, and the effect of collaboratively removing residual ammonia water pollutants is achieved.
Description
Technical field
The present invention relates to coking technology field, particularly to a kind of remained ammonia processing method and system.
Background technology
Containing ammonia, phenol, sulfide, cyanide, pyridine and tar in the ammonia that coke-oven plant's process of coking produces
Etc. poisonous and harmful substance, a part of ammonia circulation is back to coke oven coke oven uprising tube and sprays coke-stove gas, and this part is referred to as
For cyclic ammonia water, in addition to cyclic ammonia water, remained ammonia can only deliver to subsequent biochemical processing system after processing.Mesh
Before, the process of remained ammonia the most all uses steamed ammonia process, steaming process ammonia still process to be using steam as carrier,
The ammonia nitrogen dissolved in water is transferred in steam by the method utilizing distillation, thus reaches the purpose of removal of ammonia and nitrogen.
In remained ammonia, ammonia nitrogen is mainly with free ammonia (mainly (NH4)2CO3, NH4OH etc.) and Stagnant ammonium
Salt (mainly NH4Cl、(NH4)2SO4、NH4SCN etc.) two kinds of forms exist, in addition to ammonia nitrogen, residue
Possibly together with finite concentration HCN, H in ammonia2S, volatile phenol etc. are in acid material, wherein the concentration of free ammonia
Generally 2～4g/L, the concentration general 1～2g/L of fixed ammonia, free ammonia is easy from water during steam air stripping
In steam, and solid ammonium-salt is strong acid weak base salt, is difficult to decompose in water, is difficult to removing during ammonia still process,
Therefore, through adding alkali process, solid ammonium-salt to be converted into free ammonia, ammonia still process efficiency can be effectively improved.
In prior art, alkali liquor is directly added in the remained ammonia that coking produces, and is then steamed by ammonia still
Ammonia, the dosage of alkali liquor is excessive, brings bigger economic pressures to coke-oven plant, and due to ammonia in remained ammonia
It is mutually restriction, when alkali liquor dosage is more, waste water after ammonia still process between the removal effect of nitrogen and cyanide
The material concentrations such as middle cyanide, phenols then can be higher, the pollutant such as cyanide containing high concentration, phenols
Microorganism is still caused large effect after delivering to biochemical system by distilled ammonia wastewater.Visible, surplus in prior art
There is, during remaining ammonia treatment, the technical problem that alkali liquor consumption is excessive.
Summary of the invention
The embodiment of the present invention provides a kind of remained ammonia processing method and system, is used for solving to remain in prior art
The technical problem that during remaining ammonia treatment, alkali liquor consumption is excessive, reduces the consumption of alkali liquor.
The embodiment of the present application provides a kind of remained ammonia processing method, including:
The remained ammonia produced during coking is carried out the pretreatment of oil removing class, oil removal；
Pretreated remained ammonia is heated to design temperature；
Will warm up the remained ammonia of design temperature to inject the first ammonia still and carry out ammonia still process for the first time and process；
Ammonia after first time ammonia still process processes adds alkali liquor and carries out acid-base value regulation, at ammonia still process for the first time
The pH value of the ammonia after reason is adjusted to preset value, and described preset value is more than or equal to 10；
Ammonia after acid-base value being regulated inputs the second ammonia still and carries out second time ammonia still process process, it is thus achieved that after ammonia still process
Waste water.
Optionally, the described remained ammonia to producing during coking carries out the pre-place of oil removing class, oil removal
Reason, including:
The remained ammonia produced in coking is passed through ammonia precipitation process groove precipitate 4～6 hours, to remove suspension
Thing and oils；
Remained ammonia after precipitation is flowed into the standing oil removing 4 of preposition ammonia medial launder～6 hours；
Stand the remained ammonia entrance with pressure coke filter after oil removing to carry out again at oil removing class, oil removal
Reason.
Optionally, described design temperature is more than or equal to 80 DEG C.
Optionally, described pretreated remained ammonia is heated to design temperature, including:
Remained ammonia after being processed by plate type heat exchanger, spiral-plate heat exchanger or diamond heating is heated to
80 DEG C or more than.
Optionally, inject the first ammonia still at the described remained ammonia that will warm up design temperature to carry out for the first time
Before ammonia still process processes, described method also includes:
The pH value of the remained ammonia that will warm up design temperature regulates to less than 8.
Optionally, described ammonia after first time ammonia still process processes adds alkali liquor and carries out acid-base value regulation, bag
Include:
The NaOH alkali liquor adding concentration 30% in ammonia after first time ammonia still process processes carries out acid-base value tune
Joint.
Optionally, the described pH value by the ammonia after first time ammonia still process process is adjusted to preset value, including:
The pH value of the ammonia after first time ammonia still process being processed regulates to 10～10.5.
The embodiment of the present application also provides for a kind of remained ammonia processing system, including:
Pretreatment unit, for carrying out oil removing class, oil removal to the remained ammonia produced during coking
Pretreatment；
Heater, for being heated to design temperature by pretreated remained ammonia；
First ammonia still, processes for the remained ammonia being heated to design temperature carries out ammonia still process for the first time；
Ammonia medial launder, the ammonia after processing first time ammonia still process carries out acid-base value regulation, will for the first time
The pH value of the ammonia after ammonia still process process is adjusted to preset value, and described preset value is more than or equal to 10；
Second ammonia still, the ammonia after acid-base value being regulated inputs the second ammonia still and carries out second time ammonia still process
Process, it is thus achieved that the waste water after ammonia still process.
Optionally, described system also includes:
First detecting system, for detecting the acid-base value of the remained ammonia before entering described first ammonia still, control
System enters the pH value of the remained ammonia of described first ammonia still below 8；
Second detecting system, for detecting the acid-base value entering the ammonia before described second ammonia still, control into
Enter the pH value of ammonia of described second ammonia still between 10～10.5.
Optionally, described pretreatment unit includes:
Ammonia precipitation process groove, for precipitating the remained ammonia produced in coking, to go oil removal and oils；
Preposition ammonia medial launder, the remained ammonia after precipitating described ammonia precipitation process groove carries out standing and removes
Oil；
Coke filter, for carrying out oil removing class again, except outstanding to the remained ammonia of entrance with pressure after standing oil removing
Float processes.
Said one in the embodiment of the present application or multiple technical scheme, at least have the following technical effect that
The embodiment of the present application is when processing remained ammonia, and the remained ammonia removing oils and float heats
Process, by heating first by ammonium carbonate class substance decomposition relatively low for decomposition temperature in ammonia, follow-up to save
Decompose alkali liquor additional during fixed ammonia salt；Further, the ammonia after heating is first passed through the first ammonia still to enter
Row ammonia still process for the first time processes, and first removes major part HCN, CO in remained ammonia2, volatile phenol and free ammonia etc.；
Ammonia after the first ammonia still process processes adds alkali liquor and carries out acid-base value regulation, owing to having processed through first time ammonia still process
Through eliminating major part HCN, CO2, volatile phenol and free ammonia etc., so to alkali liquor when adding alkali liquor regulation again
Demand be greatly reduced；Then, the ammonia after acid-alkali accommodation is passed through in the second ammonia still carries out the second steaming
Ammonia treatment, removes solid ammonium-salt and remaining fraction HCN, volatile phenol, H2The polluters such as S, it is thus achieved that
Waste water after ammonia still process is to deliver to biochemical system, due to the cyanide reduced in waste water, the phenols of alkali liquor addition
Reduce etc. material concentration, reduce the adverse effect to microorganism, it is seen then that by the technical scheme of the application
Solve the technical problem that when remained ammonia processes in prior art, alkali liquor consumption is excessive, decrease the use of alkali liquor
Amount, reduces cost, has reached the effect of collaborative removal remained ammonia pollutant simultaneously.
Accompanying drawing explanation
The flow chart of a kind of remained ammonia processing method that Fig. 1 provides for the embodiment of the present application；
The schematic diagram of a kind of remained ammonia processing system that Fig. 2 provides for the embodiment of the present application；
Fig. 3 for the embodiment of the present application provide to remained ammonia process before and process after cyanogen root concentration schematic diagram；
Fig. 4 for the embodiment of the present application provide to remained ammonia process before and process after ammonia nitrogen concentration schematic diagram.
Detailed description of the invention
In the technical scheme that the embodiment of the present application provides, may consume by removing in advance in remained ammonia
The easy decomposed substance of alkali liquor, then addition alkali liquor removes fixed ammonia salt in remained ammonia, and then reduce alkali liquor
Usage amount, solve the technical problem that when remained ammonia processes in prior art, alkali liquor usage amount is excessive.
Below in conjunction with the accompanying drawings the embodiment of the present application technical scheme main is realized principle, detailed description of the invention and
The beneficial effect that should be able to reach is explained in detail by it.
Embodiment one
Refer to Fig. 1, the embodiment of the present application provides a kind of method that remained ammonia processes, and the method includes:
S10: the remained ammonia produced during coking is carried out the pretreatment of oil removing class, oil removal；
S20: pretreated remained ammonia is heated to design temperature；
S30: will warm up the remained ammonia of design temperature and inject the first ammonia still and carry out ammonia still process for the first time and process；
S40: add alkali liquor in the ammonia after first time ammonia still process processes and carry out acid-base value regulation, will for the first time
The pH value of the ammonia after ammonia still process process is adjusted to preset value, and described preset value is more than or equal to 10；
S50: the ammonia after acid-base value being regulated inputs the second ammonia still and carries out second time ammonia still process process, it is thus achieved that
Waste water after ammonia still process.
S10 is in order to improve the effect that the ammonia still process to remained ammonia processes, during the embodiment of the present application is to coking
The remained ammonia produced can carry out secondary removal to oils and suspended material when carrying out pretreatment.Concrete,
The remained ammonia produced in coking is first passed through ammonia precipitation process groove precipitate 4～6 hours, to remove oil removal
And oils；Then, the remained ammonia after precipitation is flowed into preposition ammonia medial launder i.e. ammonia medial launder 1, quiet
Put oil removing 4～6 hours；Then, the remained ammonia entrance with pressure coke filter after standing oil removing is carried out again
Oil removing class, oil removal process, thus remove oils and suspended material that remained ammonia carries more comprehensively.
Pretreated remained ammonia, in order to reduce the follow-up amount adding alkali, is heated to design temperature by S20.Its
In, design temperature is more than or equal to 80 DEG C, and concrete value can be 80 DEG C, 85 DEG C, 90 DEG C, 100 DEG C etc..
During heating, it is possible to use pretreated remained ammonia is heated by the self-produced waste heat in coke-oven plant, it is also possible to
Utilize tube furnace combustion heating that remained ammonia is heated, specifically can utilize plate type heat exchanger or spiral lamina
Remained ammonia is heated to 80 DEG C by heat exchangers etc., on the one hand utilizes the ammonium carbonate etc. that waste heat is relatively low to decomposition temperature
Salts substances decomposes, and so can save alkali number additional during subsequent decomposition solid ammonium-salt, the most permissible
Ensure that remained ammonia enters such as tower top temperature during the first ammonia still i.e. ammonia tower 1.
S30 will warm up the remained ammonia of design temperature and injects the first ammonia still and carry out ammonia still process for the first time and process
Before, in order to improve ammonia still process efficiency, before remained ammonia injects the first ammonia still, remained ammonia is carried out acid
Basicity detects, and the pH value that will warm up the remained ammonia of design temperature regulates to less than 8.Concrete,
If the acid-base value detected is too high, can be adjusted with spent acid during coking production, to control first
The pH value of the remained ammonia of ammonia still import department is below 8.By remained ammonia from the tower top of the first ammonia still
Inject, from passing through steam at the bottom of the tower of the first ammonia still, remove big portion in remained ammonia by steam gas stripping
Divide HCN, CO2, the material such as volatile phenol and free ammonia.
When S40 carries out acid-base value regulation to the ammonia after first time ammonia still process process, can be by the first ammonia still row
The ammonia gone out imports ammonia medial launder 2, adds concentration 30% in the ammonia after first time ammonia still process processes
NaOH alkali liquor carries out acid-base value regulation, and utilizes agitator to be stirred for uniformly, by the pH value of this ammonia
Being adjusted to preset value, wherein preset value is more than or equal to 10.Concrete, use the NaOH alkali of concentration 30%
Liquid, the pH value of the ammonia after first time ammonia still process being processed regulates to 10～10.5, it is possible to effectively control NaOH
The addition of alkali liquor, it is to avoid add too much alkali liquor.
S50 processes carrying out second time ammonia still process: the ammonia after acid-base value regulates is imported the second ammonia still i.e.
At the bottom of the tower of ammonia tower 2, at the bottom of the tower of the second ammonia still, it is passed through steam, utilizes steam gas stripping to remove major part
Solid ammonium-salt and fraction HCN, CO2, volatile phenol etc..In specific implementation process, in order to ensure entrance
The acid-base value of the ammonia of the second ammonia still, can carry out on-line monitoring to the ammonia before entering the second ammonia still,
The pH value of the ammonia controlling the second ammonia still import department controls more than 10.
In specific implementation process, it is also possible to by the first ammonia still and the second ammonia still overhead gas through dephlegmator
Deliver to claus oven combustion decomposition after dividing contracting or deliver to sulfur ammonium operation production side-product.Steamed by the second ammonia still
Obtain waste water after ammonia, this waste water is delivered to biochemical system and carries out subsequent treatment or utilization.
A kind of remained ammonia processing method provided based on above-described embodiment, the embodiment of the present application is also corresponding to be provided
A kind of remained ammonia processing system, refer to Fig. 2, and this system includes:
Pretreatment unit 21, for carrying out oil removing class, oil removal to the remained ammonia produced during coking
Pretreatment；
Heater 22, for being heated to design temperature by pretreated remained ammonia；
First ammonia still 23, processes for the remained ammonia being heated to design temperature carries out ammonia still process for the first time；
Ammonia medial launder 24, the ammonia after processing first time ammonia still process carries out acid-base value regulation, by first
The pH value of the ammonia after secondary ammonia still process process is adjusted to preset value, and described preset value is more than or equal to 10；
Second ammonia still 25, the ammonia after acid-base value being regulated inputs the second ammonia still to carry out steaming for the second time
Ammonia treatment, it is thus achieved that the waste water after ammonia still process.
Wherein, described pretreatment unit 21 includes: ammonia precipitation process groove, preposition ammonia medial launder (i.e. ammonia
Medial launder 1) and coke filter.Ammonia precipitation process groove is used for precipitating the remained ammonia produced in coking,
To go oil removal and oils；Preposition ammonia medial launder residue ammonia after described ammonia precipitation process groove is precipitated
Water carries out standing oil removing；Coke filter is for removing the remained ammonia of entrance with pressure after standing oil removing again
Oils, oil removal process.
In specific implementation process, this system also includes: the first detecting system 26 and the second detecting system 27.
First detecting system 26, for detecting the acid-base value of the remained ammonia before entering described first ammonia still, controls
Enter the pH value of remained ammonia of described first ammonia still below 8；Second detecting system 27, is used for examining
Survey the acid-base value of the ammonia before entering described second ammonia still, control the ammonia of described second ammonia still of entrance
PH value is between 10～10.5.Concrete, the first detecting system 26 and the second detecting system 27 can be
PH on-line detecting system, can automatically control ammonia still and enter the switch at ammonia, when pH value detection is up to standard
Open switch, otherwise closing switch, control to enter the pH value of remained ammonia of the first ammonia still below 8,
And enter the pH value of the ammonia of the second ammonia still between 10～10.5.
Refer to Fig. 2, the application process of the collaborative ammonia steaming system of residual coking ammonia water is as follows: remained ammonia warp
Ammonia precipitation process groove precipitates, and the sedimentation time is 4～6h, and remained ammonia after precipitation is from flowing to ammonia medial launder
1 stands oil removing, and time of repose is 4～6h, stands ammonia entrance with pressure coke filter after oil removing, coke
Filter hydraulic detention time is at about 10min.Remained ammonia is heated to 80 DEG C through heat exchanger after pretreatment
Above；PH on-line measuring device 26 is set in the first ammonia still 23 import department, controls its pH value 8
Hereinafter, waste water is flowed out at the bottom of the first ammonia still 23 tower to mixed with the stirring of 30%NaOH alkali liquor in ammonia medial launder
Enter the second ammonia still 25 top after conjunction, pH on-line measuring device is set in the second ammonia still 25 import department
27 ensure that ammonia pH value into the second ammonia still 25, more than 10, processes through the second ammonia still 25 ammonia still process
After waste water whereabouts biochemical system.
Refer to Fig. 3 and Fig. 4, before processing for using the embodiment of the present application that remained ammonia is carried out and after process
Cyanogen root concentration, ammonia nitrogen concentration schematic diagram.Wherein, after ammonia still process, Cyanide in Waste Water root concentration can reach 15mg/L substantially
Left and right, minimum up to below 10mg/L, significantly reduce compared to cyanogen root concentration before processing, and,
While cyanogen root concentration is greatly reduced, after ammonia still process, in waste water, ammonia nitrogen concentration is maintained at below 250mg/L, thus
Visible, the present invention implement after, cyanogen root concentration has met subsequent biochemical system influent quality requirement, reached with
Ammonia nitrogen concentration works in coordination with the beneficial effect of decline.
By the one or more technical schemes in the embodiment of the present application, it is possible to achieve following one or more skills
Art effect:
(1), obtain ammonia still process after waste water in ammonia nitrogen concentration is not only greatly reduced, also effectively reduce waste water
Middle HCN, H2The content of the acidic materials such as S and volatile phenol, it is to avoid add excess alkali liquor during ammonia still process and cause
Ammonia nitrogen concentration is up to standard and CN-The phenomenon the most up to standard with aldehydes matter, solves ammonia nitrogen and cyaniding in remained ammonia
Thing, volatile phenol removal effect between the difficult problem of mutual restriction, reached ammonia nitrogen and cyanide during ammonia still process,
The collaborative decline of volatile phenol, improves engineer applied and is worth.
(2), ammonia still process process be divided into two steps, control the pH value of every one-level ammonia still import department ammonia, utilize
First ammonia still removes major part HCN, CO in waste water2, volatile phenol and free ammonia etc., utilize the second ammonia still process
Tower removes major part fixed ammonia and fraction HCN, CO in waste water2, volatile phenol, ammonia nitrogen in waste water after ammonia still process
HCN、CO2, volatile phenol etc. all declines to a great extent.
(3), by heat treated, for the first time ammonia still process process and second time ammonia still process acid-base value before treatment control,
Significantly reduce the consumption of ammonia still process process additional NaOH alkali liquor.
Although preferred embodiments of the present invention have been described, but those skilled in the art once know base
This creativeness concept, then can make other change and amendment to these embodiments.So, appended right is wanted
Ask and be intended to be construed to include preferred embodiment and fall into all changes and the amendment of the scope of the invention.
Obviously, those skilled in the art can carry out various change and modification without deviating from this to the present invention
Bright spirit and scope.So, if the present invention these amendment and modification belong to the claims in the present invention and
Within the scope of its equivalent technologies, then the present invention is also intended to comprise these change and modification.
Claims (10)
1. a remained ammonia processing method, it is characterised in that including:
The remained ammonia produced during coking is carried out the pretreatment of oil removing class, oil removal；
Pretreated remained ammonia is heated to design temperature；
Will warm up the remained ammonia of design temperature to inject the first ammonia still and carry out ammonia still process for the first time and process；
Ammonia after first time ammonia still process processes adds alkali liquor and carries out acid-base value regulation, at ammonia still process for the first time
The pH value of the ammonia after reason is adjusted to preset value, and described preset value is more than or equal to 10；
Ammonia after acid-base value being regulated inputs the second ammonia still and carries out second time ammonia still process process, it is thus achieved that after ammonia still process
Waste water.
2. the method for claim 1, it is characterised in that described generation during coking is remained
Remaining ammonia carries out the pretreatment of oil removing class, oil removal, including:
The remained ammonia produced in coking is passed through ammonia precipitation process groove precipitate 4～6 hours, to remove suspension
Thing and oils；
Remained ammonia after precipitation is flowed into the standing oil removing 4 of preposition ammonia medial launder～6 hours；
Stand the remained ammonia entrance with pressure coke filter after oil removing to carry out again at oil removing class, oil removal
Reason.
3. the method for claim 1, it is characterised in that described design temperature is more than or equal to 80 DEG C.
4. method as claimed in claim 3, it is characterised in that described by pretreated remained ammonia
It is heated to design temperature, including:
Remained ammonia after being processed by plate type heat exchanger, spiral-plate heat exchanger or diamond heating is heated to
80℃。
5. the method for claim 1, it is characterised in that at the described design temperature that will warm up
Remained ammonia injects the first ammonia still and carries out before for the first time ammonia still process processes, and described method also includes:
The pH value of the remained ammonia that will warm up design temperature regulates to less than 8.
6. the method as described in Claims 1 to 5 is arbitrary, it is characterised in that described at first time ammonia still process
Ammonia after reason adds alkali liquor and carries out acid-base value regulation, including:
The NaOH alkali liquor adding concentration 30% in ammonia after first time ammonia still process processes carries out acid-base value tune
Joint.
7. method as claimed in claim 6, it is characterised in that described by after first time ammonia still process process
The pH value of ammonia is adjusted to preset value, including:
The pH value of the ammonia after first time ammonia still process being processed regulates to 10～10.5.
8. a remained ammonia processing system, it is characterised in that including:
Pretreatment unit, for carrying out oil removing class, oil removal to the remained ammonia produced during coking
Pretreatment；
Heater, for being heated to design temperature by pretreated remained ammonia；
First ammonia still, processes for the remained ammonia being heated to design temperature carries out ammonia still process for the first time；
Ammonia medial launder, the ammonia after processing first time ammonia still process carries out acid-base value regulation, will for the first time
The pH value of the ammonia after ammonia still process process is adjusted to preset value, and described preset value is more than or equal to 10；
Second ammonia still, the ammonia after acid-base value being regulated inputs the second ammonia still and carries out second time ammonia still process
Process, it is thus achieved that the waste water after ammonia still process.
9. system as claimed in claim 8, it is characterised in that described system also includes:
First detecting system, for detecting the acid-base value of the remained ammonia before entering described first ammonia still, control
System enters the pH value of the remained ammonia of described first ammonia still below 8；
Second detecting system, for detecting the acid-base value entering the ammonia before described second ammonia still, control into
Enter the pH value of ammonia of described second ammonia still between 10～10.5.
10. system as claimed in claim 9, it is characterised in that described pretreatment unit includes:
Ammonia precipitation process groove, for precipitating the remained ammonia produced in coking, to go oil removal and oils；
Preposition ammonia medial launder, the remained ammonia after precipitating described ammonia precipitation process groove carries out standing and removes
Oil；
Coke filter, for carrying out oil removing class again, except outstanding to the remained ammonia of entrance with pressure after standing oil removing
Float processes.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110862197A (en) * | 2019-12-06 | 2020-03-06 | 太原理工大学 | Method and device for treating residual ammonia water in coking industry |
| CN112551793A (en) * | 2020-12-10 | 2021-03-26 | 天津大学 | Ammonia distillation method and device for ammonia-containing wastewater |
| CN113105051A (en) * | 2021-03-31 | 2021-07-13 | 江苏瑞达环保科技有限公司 | Method for controlling liquid caustic soda addition in ammonia distillation process based on conductivity change |
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| CN101941720A (en) * | 2010-08-23 | 2011-01-12 | 天津市创举科技有限公司 | Tube furnace ammonia evaporation process and equipment |
| CN103342401A (en) * | 2013-07-24 | 2013-10-09 | 武汉钢铁(集团)公司 | Stepwise ammonia distilling method for coking residual ammonia wastewater |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101941720A (en) * | 2010-08-23 | 2011-01-12 | 天津市创举科技有限公司 | Tube furnace ammonia evaporation process and equipment |
| CN103342401A (en) * | 2013-07-24 | 2013-10-09 | 武汉钢铁(集团)公司 | Stepwise ammonia distilling method for coking residual ammonia wastewater |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110862197A (en) * | 2019-12-06 | 2020-03-06 | 太原理工大学 | Method and device for treating residual ammonia water in coking industry |
| CN112551793A (en) * | 2020-12-10 | 2021-03-26 | 天津大学 | Ammonia distillation method and device for ammonia-containing wastewater |
| CN113105051A (en) * | 2021-03-31 | 2021-07-13 | 江苏瑞达环保科技有限公司 | Method for controlling liquid caustic soda addition in ammonia distillation process based on conductivity change |
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