CN109250854A - The processing method of semi-coke wastewater - Google Patents
The processing method of semi-coke wastewater Download PDFInfo
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- CN109250854A CN109250854A CN201810934435.1A CN201810934435A CN109250854A CN 109250854 A CN109250854 A CN 109250854A CN 201810934435 A CN201810934435 A CN 201810934435A CN 109250854 A CN109250854 A CN 109250854A
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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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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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
- C02F1/40—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
- C02F2001/5218—Crystallization
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Abstract
The present invention provides a kind of processing method of semi-coke wastewater comprising following steps: the isolated tar of semi-coke wastewater and detar waste water；Adjust the pH value of detar waste water and the access negative pressure deammoniation tower after preheating, low-pressure steam accesses negative pressure deammoniation tower tower bottom, Z-type column plate is equipped in negative pressure deammoniation tower, detar waste water is using low-pressure steam as heat source, and successively boiling injection deamination obtains ammonia steam and deamination waste water under the action of Z-type column plate, deamination waste water flows out through negative pressure deammoniation tower tower bottom and carries out heat exchange for the detar waste water of 9-12 with pH value to preheat detar waste water, boiling temperature of the detar waste water in negative pressure deammoniation tower is 60-75 DEG C, pressure≤0.25Mpa of low-pressure steam；Deamination waste water after preheating detar waste water is concentrated to form condensed water through dephenolize tower, and water crystallization and isolated phenates and lye is concentrated.The processing method of semi-coke wastewater provided by the invention not only can effectively recycle tar, ammonia and phenol in waste water, but also high treating effect, operating cost are low.
Description
Technical field
The present invention relates to technical field of water pollution treatment, specifically, being related to a kind of processing method of semi-coke wastewater.
Background technique
Semi-coke be using jet coal, dross coal or weakly caking coal as raw material, middle low temperature (about 650 DEG C) carbonization obtain compared with
Low volatile solids charcoal metallic substance, also known as semicoke.Semi-coke have high fixed carbon, high specific resistance, high chemical characteristic feature, extensively
Applied to industries such as calcium carbide, ferroalloy, chemical fertilizer gas-making, blast furnace blowing and civilian clean type coal manufactures.Semi-coke wastewater is mainly orchid
Dedusting washing water in charcoal production process, the condensed water in raw coke oven gas and remained ammonia etc..It is dry with (about 1000 DEG C) of coke high-temperature
It evaporates technique to compare, low temperature distillation removing fugitive constituent coal gas generated is waste without high temperature second pyrolysis in semi-coke production technology
Containing a large amount of not by the pollutant of high-temperature oxydation in Coal-gas Washing Water Using, concentration is higher by 10 times or so than coking wastewater.
Currently, domestic processing semi-coke wastewater often uses the following two kinds mode:
One, biochemical treatment: the composition of coking wastewater is especially complex, and biodegradability is low, and the zero-emission often said, is only processing
Waste water afterwards is reused in production (such as in terms of quenching), is only that waste water is become exhaust gas to be discharged into atmosphere when being used for quenching,
It also will cause pollution；
Two, burning disposal: waste water is injected directly into the flame of gas-fired, chemically for basic principle, belongs to imperfect combustion,
A large amount of CO certainly will be generated, and can not be completely removed for partial organic substances such as ammonia and cyanogen, and a large amount of CO is needed 1100
At DEG C there are the time be 1s, can just be oxidized to CO2, in addition incinerator occupied area is very big, and the heat of burning is unable to fully benefit again
Utilization can not be gone again with, water, causes the significant wastage of the energy and water, while being safeguarded and operating cost is higher, in burning disposal mistake
Cheng Zhong, contained cyanide and part ammonia cyanide are discharged in atmosphere again after can not being handled, and cause atmosphere pollution.
Above two kinds of methods are there are one common shortcoming, i.e., some useful components in waste water, as tar, phenol,
Ammonia etc. is not recycled, and recycle resource cannot, this not only causes the significant waste of resource, also polluted environment.
Therefore, it is necessary to provide a kind of processing method of new semi-coke wastewater to avoid the above problem.
Summary of the invention
In order to solve the above technical problem, the present invention provides a kind of processing method of semi-coke wastewater, this method not only can be with
Tar, ammonia and phenol effectively in recycling waste water, and high treating effect, operating cost are low.
Technical scheme is as follows:
A kind of processing method of semi-coke wastewater, comprising the following steps:
Oil removing: semi-coke wastewater obtains tar and detar waste water through gravity settling separation in raw water vessel；
Deamination: detar waste water is adjusted to after pH value is 9-12 and is preheated, the detar waste water after preheating accesses negative pressure deammoniation tower
Negative pressure deammoniation tower tower bottom is accessed from extraneous low-pressure steam, wherein Z-type column plate is equipped in negative pressure deammoniation tower, after preheating in top
Detar waste water using low-pressure steam as heat source, and under the action of Z-type column plate successively boiling injection deamination obtain ammonia steam and
Deamination waste water, deamination waste water flow out through negative pressure deammoniation tower tower bottom and carry out heat exchange for the detar waste water of 9-12 with pH value with pre-
Hot detar waste water, boiling temperature of the detar waste water in negative pressure deammoniation tower are 60-75 DEG C, the pressure of low-pressure steam≤
0.25Mpa；
Dephenolize: the deamination waste water after preheating detar waste water is concentrated to form condensed water through dephenolize tower, and condensed water reaches concentration temperature
Spend the saturation degree of lower phenates, concentration water crystallization and isolated phenates and lye, wherein phenates is reacted with carbon dioxide in filler
Reaction obtains crystallization crude phenols in tower reaction and sodium bicarbonate, the steam that generation is concentrated are discharged after condensing.
Preferably, in deoiling step, semi-coke wastewater is heated to 45-55 DEG C in advance.
Preferably, it is equipped with coil pipe in raw water vessel, the steam of generation is concentrated through coil pipe and semi-coke wastewater heat exchange with will be blue
Charcoal waste water is heated to 80-85 DEG C.
Preferably, dephenolize tower is equipped with N number of, and the deamination waste water after preheating detar waste water is successively concentrated through multiple dephenolize towers,
And by the flow direction of the deamination waste water after preheating detar waste water, the steam that the concentration of m-th dephenolize tower generates enters M+1
The heat source that dephenolize tower is evaporated as deamination waste water, wherein N is the integer greater than 1, and M is the integer not less than 1, and less than N.
Preferably, in deoiling step, the detar waste water flowed out from raw water vessel also passes through more medium filter mistake
Filter, more medium filter retain profiling oil droplet and detar waste water are discharged.
Preferably, more medium filter is by controlling the backwash of its import and export pressure difference, and flushing water enters raw water vessel and removes
Oil.
Preferably, before detar waste water access negative pressure deammoniation tower, 0-40 mg denitrogenation is added also in every liter of detar waste water
Agent, wherein denitrifier contains at least one of O, H, OH, CH, CH2 atom and ion activity group.
Preferably, it in dephenolize step, is concentrated after water crystallization and phenates is obtained by centrifuge separation or/and gravity settling separation
And lye.
Preferably, before deoiling step, semi-coke wastewater is filtered to remove bulky grain sundries.
The processing method of semi-coke wastewater provided in an embodiment of the present invention has following technical effect that the processing of semi-coke wastewater
Method, comprising the following steps: oil removing: semi-coke wastewater obtains tar through gravity settling separation in raw water vessel and detar is useless
Water；Deamination: detar waste water is adjusted to after pH value is 9-12 and is preheated, the detar waste water after preheating accesses negative pressure deamination tower top
Portion accesses negative pressure deammoniation tower tower bottom from extraneous low-pressure steam, wherein Z-type column plate is equipped in negative pressure deammoniation tower, after preheating
Detar waste water is using low-pressure steam as heat source, and successively boiling injection deamination obtains ammonia steam and takes off under the action of Z-type column plate
Ammonia waste water, deamination waste water flows out through negative pressure deammoniation tower tower bottom and carries out heat exchange with the detar waste water to be given up with preheating detar
Water, boiling temperature of the detar waste water in negative pressure deammoniation tower are 60-75 DEG C, pressure≤0.25Mpa of low-pressure steam；Dephenolize:
Deamination waste water after preheating detar waste water is concentrated to form condensed water through dephenolize tower, and condensed water reaches phenates under thickening temperature
Saturation degree, concentration water crystallization and isolated phenates and lye, wherein phenates is anti-in filler reaction tower reacts with carbon dioxide
It should obtain crystallization crude phenols and sodium bicarbonate, the steam that generation is concentrated are discharged after condensing.Waste water not only can effectively be recycled
In tar, ammonia and phenol, and high treating effect, operating cost are low.
Detailed description of the invention
To describe the technical solutions in the embodiments of the present invention more clearly, make required in being described below to embodiment
Attached drawing is briefly described, it should be apparent that, drawings in the following description are only some embodiments of the invention, for
For those of ordinary skill in the art, without creative efforts, it can also be obtained according to these attached drawings other
Attached drawing, in which:
Fig. 1 is the structural block diagram of semi-coke wastewater processing system of the invention；
Fig. 2 is the structural block diagram of degreasing unit in semi-coke wastewater processing system shown in Fig. 1；
Fig. 3 is the structural block diagram of deamination apparatus in semi-coke wastewater processing system shown in Fig. 1；
Fig. 4 is the structural block diagram of dephenolize device in semi-coke wastewater processing system shown in Fig. 1；
Fig. 5 is the flow chart of the processing system, method of semi-coke wastewater of the invention.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that the described embodiments are merely a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts all other
Embodiment shall fall within the protection scope of the present invention.
It should be noted that the connection in following implementation is to be connected by pipeline, to realize that liquid is being connected
Two components between flowing.
Fig. 1-Fig. 4 is please referred to, semi-coke wastewater processing system 100 includes sequentially connected degreasing unit 1, deamination apparatus
3 and dephenolize device 5.
Degreasing unit 1 includes raw water vessel 11, the liquid pump 13 connecting with raw water vessel 11 and light oil pool 15 and heavy oil pond 17,
Raw water vessel 11 has the top overflow port connecting with the light oil pool 15 and the lower part overflow port connecting with the heavy oil pond 17.
In the present embodiment, degreasing unit 1 further includes more medium filter 19, and more medium filter 19 connects raw water vessel 11 and deamination
Device 3.
Deamination apparatus 3 includes the collecting-tank 31 connecting with more medium filter 19, pipe-line mixer 32, molten alkali pool 33, heat
Parallel operation 34, deamination pond 35, negative pressure deammoniation tower 36, ammonia recovery unit 37, condenser 38, gas-liquid separator 39 and tank used for storing ammonia
30.Pipe-line mixer 32 is connect with collecting-tank 31, molten alkali pool 33 and heat exchanger 34 respectively, deamination pond 35 and negative pressure deammoniation tower 36
It is connect respectively with heat exchanger 34, dephenolize device 5 is also connected on deamination pond 35, is also connected with condenser on negative pressure deammoniation tower 36
38 and gas-liquid separator 39, gas-liquid separator 39 connect with condenser 38, be also connected with ammonia recovery unit in turn on condenser 38
37 and tank used for storing ammonia 30.Wherein, elevator pump 3A, pipe-line mixer 32 and molten alkali are equipped between pipe-line mixer 32 and collecting-tank 31
It is equipped between pond 33 plus alkali pump 3B, the water outlet of negative pressure deammoniation tower 36 is equipped with the water outlet of connection negative pressure deammoniation tower 36 and heat exchanger 34
3C is pumped, the water outlet of gas-liquid separator 39 is equipped with the reflux pump 3D of connection negative pressure deammoniation tower 36 and gas-liquid separator 39.
Dephenolize device 5 includes sequentially connected multiple dephenolize towers 51 and condensing tower 53.As shown, dephenolize tower 51 is equipped with three
It is a, it is followed successively by level-one dephenolize tower 51a, second level dephenolize tower 51b and three-level dephenolize tower 51c, wherein level-one dephenolize tower 51a and deamination
Pond 35 connects, and three-level dephenolize tower 51c is connect with condensing tower 53.In the present embodiment, coil pipe 111 is equipped in raw water vessel 11,
Coil pipe 111 is set between three-level dephenolize tower 51c and condensing tower 53.
The processing method of the semi-coke wastewater the following steps are included:
Oil removing: semi-coke wastewater obtains tar and detar waste water through gravity settling separation in raw water vessel 11.Specifically, it works
When, semi-coke wastewater enters raw water vessel 11 under the action of liquid pump 13, and stops 32-72h so that coke in raw water vessel 11
Oil and detar waste water separate under the effect of gravity, wherein tar light oil is expelled to gently by the top overflow port of raw water vessel 11
Oil sump 15, heavy tar are expelled to heavy oil pond 17 by the lower part overflow port of raw water vessel 11.In the present embodiment, from raw water vessel
The detar waste water flowed out in 11 also passes through more medium filter filtering 19, and more medium filter 19 retains profiling oil droplet and will take off
Tar and waste water is expelled to collecting-tank 31；Further, more medium filter 19 is backwashed by controlling its import and export pressure difference, and
Flushing water enters 11 oil removing of raw water vessel.
Deamination: detar waste water being adjusted to after pH value is 9-12 and is preheated, and the detar waste water access negative pressure after preheating is de-
36 top of ammonia tower, accesses 36 tower bottom of negative pressure deammoniation tower from extraneous low-pressure steam, wherein Z-type is equipped in negative pressure deammoniation tower 36
Column plate, the detar waste water after preheating is using low-pressure steam as heat source, and successively boiling injection deamination under the action of Z-type column plate
Ammonia steam and deamination waste water are obtained, deamination waste water flows out through 36 tower bottom of negative pressure deammoniation tower and carries out hot friendship with the detar waste water
It changes to preheat detar waste water, boiling temperature of the detar waste water in negative pressure deammoniation tower 36 is 60-75 DEG C, the pressure of low-pressure steam
Power≤0.25Mpa.Specifically, the detar waste water in collecting-tank 31 and the lye in molten alkali pool 33 are respectively by corresponding promotion
Pumping 3A and alkali pump 3B is added to be promoted to pipe-line mixer 32 so that detar waste water is adjusted to pH value is 9-12(for example, it may be PH
Value is 9, pH value 10, pH value 11, pH value are 12 etc.), the detar waste water that pH value is 9-12 is after the preheating of heat exchanger 34
Into 36 top of negative pressure deammoniation tower, 36 tower bottom of negative pressure deammoniation tower is accessed from extraneous low-pressure steam, to realize low-pressure steam
It carries out blowing ammonia in a counter-current fashion with the detar waste water after preheating, and the detar waste water after preheating is in the effect of Z-type column plate
Lower successively boiling injection deamination obtains ammonia steam and deamination waste water, and under the action of water outlet pump 3C, deamination waste water is through negative pressure deamination
36 tower bottom of tower flows out to heat exchanger 34 to carry out heat exchange with pH value for the detar waste water of 9-12.Due to liquid phase boiling point under negative pressure
Low, deamination temperature is reduced during deamination, enables whole system high-efficient deamination under relative low temperature state；Simultaneously as
Existing difference between the actual concentrations and equilibrium concentration of contained ammonia nitrogen in waste water, in the case where pH value is the alkaline condition of 9-12 with low
Pressure steam and detar waste water carry out blowing ammonia in a counter-current configuration, are transferred to the volatile substances such as the ammonia nitrogen in waste water constantly by liquid phase
In gas phase, to achieve the purpose that remove ammonia nitrogen from waste water；And pH value be 9-12 alkaline condition under, be conducive to destroy molten
The binding force between NH3 and hydrone in Xie Yushui, so as to reduce the nitrogen content after denitrogenation in waste water.
Dephenolize: the deamination waste water after preheating detar waste water forms condensed water through the concentration of dephenolize tower 51, and condensed water reaches
The saturation degree of phenates under thickening temperature, concentration water crystallization and isolated phenates and lye, wherein phenates and carbon dioxide are being filled out
Reaction obtains crystallization crude phenols in material reaction tower reaction and sodium bicarbonate, the steam that generation is concentrated are discharged after condensing.Specifically, dense
Shrink the crystallisation by cooling in crystallizing tower 53.
Lye can choose sodium hydroxide or potassium hydroxide etc..This is not especially limited.
As an implementation, in deoiling step, semi-coke wastewater is heated to 45-55 DEG C to reach demulsification mesh in advance
's.In the present embodiment, coil pipe 111 is equipped in raw water vessel 11, the steam that generation is concentrated is handed over through coil pipe 111 and semi-coke wastewater heat
It changes so that semi-coke wastewater is heated to 80-85 DEG C.The heat that can use in system in this way realizes heating demulsification type, so as to save
Demulsifier and system thermal is made full use of to reduce operating cost.
In the present embodiment, dephenolize tower 51 is equipped with N number of, and the deamination waste water after preheating detar waste water is successively through multiple dephenolizes
Tower 51 be concentrated, and by preheating detar waste water after deamination waste water flow direction, m-th dephenolize tower concentration generate steam into
Enter the heat source that the M+1 dephenolize tower is evaporated as deamination waste water, wherein N is integer greater than 1, and M is and to be less than N not less than 1
Integer.As shown in figure 4, dephenolize tower 51 is three, wherein the steam that three-level dephenolize tower 51c dephenolize concentration generates enters coil pipe
111 with semi-coke wastewater heat exchange, the steam after heat exchange is discharged after cooling.
In the present embodiment, before detar waste water access negative pressure deammoniation tower 36,0- also is added in every liter of detar waste water
40 mg denitrifiers, wherein denitrifier contains at least one of O, H, OH, CH, CH2 atom and ion activity group.Due to denitrogenation
The atoms such as O, H, OH, CH, the CH2 contained in agent and ion activity group can destroy hydrone and the intermolecular binding force of NH3, from
And NH3 molecule almost all when denitrogenation is made to be separated from the water out.In the range of 0-40 mg/L, with the increasing of additive amount
More, the nitrogen content in the water outlet of 36 water outlet of negative pressure deammoniation tower is lower, when more than 40 mg/L, with increasing for additive amount, negative pressure
Nitrogen content in the water outlet of 36 water outlet of deammoniation tower is without significant change.
In the present embodiment, it in dephenolize step, is obtained after water crystallization is concentrated by centrifuge separation or/and gravity settling separation
To phenates and lye.
In the present embodiment, before deoiling step, semi-coke wastewater is filtered to remove bulky grain sundries, wherein bulky grain is miscellaneous
Object is mainly coke powder, coal dust, the tar micelle etc. to suspend, these suspended matters are easy to precipitate in oil removing, deamination and dephenolize,
To be easy to cause line clogging.Specifically, semi-coke wastewater stores after grid, strainer etc. remove bulky grain sundries to raw water
In container.
It is found through overtesting, steam condensate (SC) is substantially free of the calcium ions and magnesium ions for leading to increase water hardness, and its amount containing phenol
Lower than 25mg/L, it is lower than 10mg/L containing ammonia nitrogen；It is 50-90kg/t waste water using the consumption consumption of steam used in negative pressure deamination, on year-on-year basis often
Pressure or pressurization deamination can save steam and consume consumption for 50-80kg/t waste water, and ammonia nitrogen removal frank >=99.9%, the ammonia nitrogen rate of recovery
Up to 99.9%.
The processing method of semi-coke wastewater provided by the above embodiment at least has following technical effect that the place of semi-coke wastewater
Reason method, comprising the following steps: oil removing: semi-coke wastewater obtains tar and detar through gravity settling separation in raw water vessel
Waste water；Deamination: detar waste water is adjusted to after pH value is 9-12 and is preheated, the detar waste water after preheating accesses negative pressure deammoniation tower
Negative pressure deammoniation tower tower bottom is accessed from extraneous low-pressure steam, wherein Z-type column plate is equipped in negative pressure deammoniation tower, after preheating in top
Detar waste water using low-pressure steam as heat source, and under the action of Z-type column plate successively boiling injection deamination obtain ammonia steam and
Deamination waste water, deamination waste water flow out through negative pressure deammoniation tower tower bottom and carry out heat exchange with the detar waste water to preheat detar
Waste water, boiling temperature of the detar waste water in negative pressure deammoniation tower are 60-75 DEG C, pressure≤0.25Mpa of low-pressure steam；It is de-
Phenol: the deamination waste water after preheating detar waste water is concentrated to form condensed water through dephenolize tower, and condensed water reaches phenol under thickening temperature
The saturation degree of salt, concentration water crystallization and isolated phenates and lye, wherein phenates is reacted with carbon dioxide in filler reaction tower
Middle reaction obtains crystallization crude phenols and sodium bicarbonate, the steam that generation is concentrated are discharged after condensing.It not only can effectively recycle
Tar, ammonia and phenol in waste water, and high treating effect, operating cost are low.
More than, it is only presently preferred embodiments of the present invention, is not intended to limit the present invention in any form, although this
Invention has been disclosed in a preferred embodiment above, and however, it is not intended to limit the invention, any person skilled in the art,
It does not depart within the scope of technical solution of the present invention, when the technology contents using the disclosure above make a little change or are modified to equivalent
The equivalent embodiment of variation, but without departing from the technical solutions of the present invention, according to the technical essence of the invention to the above reality
Any simple modification, equivalent change and modification made by example are applied, all of which are still within the scope of the technical scheme of the invention.
Claims (9)
1. a kind of processing method of semi-coke wastewater, which comprises the following steps:
Oil removing: semi-coke wastewater obtains tar and detar waste water through gravity settling separation in raw water vessel；
Deamination: detar waste water is adjusted to after pH value is 9-12 and is preheated, the detar waste water after preheating accesses negative pressure deammoniation tower
Negative pressure deammoniation tower tower bottom is accessed from extraneous low-pressure steam, wherein Z-type column plate is equipped in negative pressure deammoniation tower, after preheating in top
Detar waste water using low-pressure steam as heat source, and under the action of Z-type column plate successively boiling injection deamination obtain ammonia steam and
Deamination waste water, deamination waste water flow out through negative pressure deammoniation tower tower bottom and carry out heat exchange for the detar waste water of 9-12 with pH value with pre-
Hot detar waste water, boiling temperature of the detar waste water in negative pressure deammoniation tower are 60-75 DEG C, the pressure of low-pressure steam≤
0.25Mpa；
Dephenolize: the deamination waste water after preheating detar waste water is concentrated to form condensed water through dephenolize tower, and condensed water reaches concentration temperature
Spend the saturation degree of lower phenates, concentration water crystallization and isolated phenates and lye, wherein phenates is reacted with carbon dioxide in filler
Reaction obtains crystallization crude phenols in tower reaction and sodium bicarbonate, the steam that generation is concentrated are discharged after condensing.
2. the processing method of semi-coke wastewater according to claim 1, which is characterized in that, in advance will be blue in deoiling step
Charcoal waste water is heated to 45-55 DEG C.
3. the processing method of semi-coke wastewater according to claim 2, which is characterized in that coil pipe is equipped in raw water vessel, it is dense
The steam that contracting generates is through coil pipe and semi-coke wastewater heat exchange semi-coke wastewater is heated to 80-85 DEG C.
4. the processing method of semi-coke wastewater according to claim 3, which is characterized in that dephenolize tower is equipped with N number of, preheating decoking
Deamination waste water after oily waste water is successively concentrated through multiple dephenolize towers, and by the flowing side of the deamination waste water after preheating detar waste water
The steam generated to the concentration of, m-th dephenolize tower enters the heat source that the M+1 dephenolize tower is evaporated as deamination waste water, wherein N is
Integer greater than 1, M are the integer not less than 1, and less than N.
5. the processing method of semi-coke wastewater according to claim 1, which is characterized in that in deoiling step, hold from raw water
The detar waste water flowed out in device also passes through more medium filter filtering, and more medium filter retains profiling oil droplet and by detar
Waste water discharge.
6. the processing method of semi-coke wastewater according to claim 5, which is characterized in that more medium filter is by controlling it
The backwash of import and export pressure difference, and flushing water enters raw water vessel oil removing.
7. the processing method of semi-coke wastewater according to claim 1, which is characterized in that in deamination step, detar is useless
Water access negative pressure deammoniation tower before, also in every liter of detar waste water be added 0-40 mg denitrifier, wherein denitrifier contain O, H,
At least one of OH, CH, CH2 atom and ion activity group.
8. the processing method of semi-coke wastewater according to claim 1, which is characterized in that in dephenolize step, condensed water knot
Phenates and lye are obtained by centrifuge separation or/and gravity settling separation after crystalline substance.
9. the processing method of semi-coke wastewater according to claim 1, which is characterized in that before deoiling step, filter semi-coke
Waste water is to remove bulky grain sundries.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110330988A (en) * | 2019-07-25 | 2019-10-15 | 内蒙古万众炜业科技环保股份公司 | A kind of wholegrain diameter coal cracking sub-prime utilizes production technology |
| CN110498564A (en) * | 2019-08-20 | 2019-11-26 | 石家庄惠洁科技有限公司 | A kind of coking, semi-coke wastewater low-cost high-efficiency treatment process |
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| CN113754171A (en) * | 2021-09-27 | 2021-12-07 | 江苏沃德凯环保科技有限公司 | Semi-coke wastewater treatment method combining rectification and membrane separation |
| CN113772870A (en) * | 2021-09-27 | 2021-12-10 | 江苏沃德凯环保科技有限公司 | Semi-coke wastewater short-process treatment method |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110330988A (en) * | 2019-07-25 | 2019-10-15 | 内蒙古万众炜业科技环保股份公司 | A kind of wholegrain diameter coal cracking sub-prime utilizes production technology |
| CN110498564A (en) * | 2019-08-20 | 2019-11-26 | 石家庄惠洁科技有限公司 | A kind of coking, semi-coke wastewater low-cost high-efficiency treatment process |
| CN113121054A (en) * | 2020-01-15 | 2021-07-16 | 王树岩 | Semi-coke wastewater treatment method |
| CN114106900A (en) * | 2020-08-28 | 2022-03-01 | 上海梅山钢铁股份有限公司 | Semi-coke-containing mixed fuel for blast furnace injection and preparation method thereof |
| CN112390445A (en) * | 2020-10-30 | 2021-02-23 | 新疆宣力环保能源有限公司 | Method and system for treating phenol-ammonia wastewater |
| CN112390445B (en) * | 2020-10-30 | 2023-04-18 | 新疆宣力环保能源有限公司 | Method and system for treating phenol-ammonia wastewater |
| CN112299513A (en) * | 2020-11-06 | 2021-02-02 | 内蒙古万众炜业科技环保股份公司 | Ammonia distillation and dephenolization coupling device and process for wastewater for semi-coke production |
| CN113754171A (en) * | 2021-09-27 | 2021-12-07 | 江苏沃德凯环保科技有限公司 | Semi-coke wastewater treatment method combining rectification and membrane separation |
| CN113772870A (en) * | 2021-09-27 | 2021-12-10 | 江苏沃德凯环保科技有限公司 | Semi-coke wastewater short-process treatment method |
| CN113772870B (en) * | 2021-09-27 | 2023-08-15 | 榆林新沃德凯环保科技有限公司 | Short-process treatment method for semi-coke wastewater |
| CN116969638A (en) * | 2023-08-30 | 2023-10-31 | 江苏沃德凯环保科技有限公司 | Deamination treatment method of semi-coke wastewater |
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