CN109485121A - The method of distilled ammonia wastewater oil removing - Google Patents
The method of distilled ammonia wastewater oil removing Download PDFInfo
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- CN109485121A CN109485121A CN201811490468.8A CN201811490468A CN109485121A CN 109485121 A CN109485121 A CN 109485121A CN 201811490468 A CN201811490468 A CN 201811490468A CN 109485121 A CN109485121 A CN 109485121A
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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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- Hydrology & Water Resources (AREA)
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- Water Treatment By Sorption (AREA)
Abstract
The present invention relates to a kind of distilled ammonia wastewaters to remove oil treatment process, mainly solves in distilled ammonia wastewater the technical issues of oil content is high, influences subsequent ammonia still process equipment and biochemical device operation discharge.The present invention is filled with the adsorption tower of adsorbent by the way that oil-containing distilled ammonia wastewater to be sent into, wherein the adsorbent is adsorbent of molecular sieve；Purified water is sent into tank, and technical solution of a part as cooling water reuse solves above-mentioned technical problem.The processing method can be used for Treatment of Coking Effluent industrial process stream.
Description
Technical field
The invention belongs to the deoiling methods of distilled ammonia wastewater in Treatment of Coking Effluent field, especially coking wastewater.
Background technique
Coking wastewater mostlys come from the subtractive process of coking, gas purification and chemical products, for high concentration containing phenol, cyanogen,
The waste water of oil, ammonia nitrogen and toxic organics, wherein using remained ammonia as main source.Remained ammonia passes through the steaming after ammonia still process
Ammonia waste water still contains the no small tar of concentration.When tar, phenol cyanogen substance enter biochemical treatment apparatus, biology can be significantly inhibited
Activity influences final wastewater treatment efficiency.The current difficulty in treatment of distilled ammonia wastewater be how effectively to be removed from waste water it is highly concentrated
The total phenol of degree, and the precondition for solving the difficult point is first to solve the oil removing problem before dephenolize.Pre-process oil removing Resolving probiems
Afterwards, solvent dephenolize can be only achieved target, and the COD in waste water is substantially reduced, into biochemical system waste water ammonia nitrogen and
COD index is effectively controlled, sewage treatment each unit stable operation.Therefore, load, coking are handled in order to mitigate biochemical system
The effective qualified discharge of waste water or recycling need to carry out oil removing advanced treating to distilled ammonia wastewater.
Absorption method is as a kind of common method for treating water, by the adsorptivity using porous solid, to handle in water
Pollutant has the advantages that applied widely, treatment effect is obvious, process is simple and recyclable utility, therefore
Water treatment field has obtained more and more concerns.Most common adsorbent is active carbon, and active carbon is since usage amount is big,
Regeneration is difficult, mostly as the supplementary means of other wastewater treatments, such as is combined etc. with membrane technology combination, with ozone.
Chinese patent CN201610611939.0 is related to a kind of wastewater treatment equipment, and the wastewater treatment equipment is by filtering
Pond, evaporation tank and active carbon water treating pond composition, filtering bottom of pond portion and evaporation tank top are connected, evaporation tank top surface and active carbon water
Processing pond top surface is connected, and coarse filtration film and refined filtration film are equipped in the filtering ponds, and the evaporation bottom of pond portion is equipped with heating device, evaporation
One lateral roof of pond is equipped with fan, is equipped with active carbon water process layer, active carbon water treating pond bottom in the active carbon water treating pond
Equipped with discharge outlet；Sufficiently, when COD is 600mg/L in waste water, the removal rate of COD is 80-90% for filtering；When COD is lower than in waste water
The removal rate of 500 mg/L, COD are 90-99%.This method does not mention the effect of the oil removing of active carbon energy and oil removing.
Chinese patent 201210119762.4 discloses the renewable difficult biology of Powdered Activated Carbon processing that recycles of one kind and drops
Solve the PACT new process of waste water, comprising the following steps: 1) Powdered Activated Carbon to precipitate in secondary settling tank and biology is living
Property sludge extraction；2) Powdered Activated Carbon and biological activated sludge of step 1) extraction are carried out dehydrating；3) to step
2) the dewatered Powdered Activated Carbon and biological activated sludge obtained be successively dried, destructive distillation and activation processing, keeps powder living
Property charcoal absorption organic matter decompose volatilization, biological activated sludge pyrolysis be active carbon；4) product for obtaining step 3) is milled
It is used afterwards as regeneration Powdered Activated Carbon investment biochemistry pool.In the present invention, after Powdered Activated Carbon is dehydrated with biological activated sludge
It is regenerated through drying, destructive distillation and activation processing, while biological activated sludge pyrolysis is active carbon, and it is living to have reached recycling powder
The purpose of property charcoal and biological activated sludge, greatly reduces the operating cost of PACT technique.The process requirement will be inhaled with sludge pump
The Powdered Activated Carbon of attached saturation is extracted out from wing, and cesspool needs to drain water when extracting Powdered Activated Carbon, to regenerating active carbon, is returned
Could put into operation again after filling out, time-consuming, this will lead to the cesspool long period stop work and make sewage disposal system without
Method operates normally.It is unable to satisfy the demand of sewage disposal system continuous operation.
Chinese patent 201510548775.7 discloses a kind of ozone, organic in active carbon combination processing high slat-containing wastewater
The method of object, method includes the following steps: after raw wastewater is aoxidized by ozone bubbling form, according to residual in waste water
The amount of the organic matter stayed using the organic matter in appropriate excessive activated carbon adsorption waste water, when activated carbon adsorption carry out auxiliary plus
Heat.The method of the present invention can effectively remove the organic matter in high slat-containing wastewater, and the removal rate of COD can be tall and big by 99.6%, decolourize to water quality
Effect is obvious, and can significantly reduce the dosage of active carbon.This method does not mention the effect of the oil removing of active carbon energy and oil removing, and living
Property charcoal and ozone be combined, power consumption is big, the high requirements on the equipment, is easy to happen ozone leakage, causes secondary pollution.
In above-mentioned document, the report using tar in molecular sieve absorption distilled ammonia wastewater is not all disclosed.
Summary of the invention
The technical problem to be solved by the present invention is to the high technical problems of oil content in distilled ammonia wastewater, provide a kind of ammonia still process
The method of oil removing in waste water, the processing method have process short, and low equipment investment, regeneration is simple, and low energy consumption, industrializing implementation
Strong advantage.
In order to solve the above technical problems, a kind of method that the present invention uses distilled ammonia wastewater oil removing, comprising the following steps:
A) the oil-containing distilled ammonia wastewater of coke-oven plant is sent into the adsorption tower for being filled with crystallite adsorbent,
B) distilled ammonia wastewater after adsorbing is sent into wastewater biochemical pond,
C) adsorbent after adsorption saturation, with being continued to use after 50 ~ 400 DEG C of nitrogen regeneration.
In the above-mentioned technical solutions, preferred technical solution, it includes X-type molecular sieve, Y that the adsorbent of molecular sieve, which is selected from,
Type molecular sieve, A type molecular sieve, TS-1, Ti-MWW, Ti-MOR, ZSM type molecular sieve, modenite, beta molecular sieve, SAPO type point
Sub- sieve, MCM-22, MCM-49, MCM-56, ZSM-5/ modenite, ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/ modenite,
ZSM-5/Magadiite, ZSM-5/ β zeolite/modenite, ZSM-5/ β zeolite/Y zeolite or ZSM-5/Y zeolite/modenite
At least one of.
In the above-mentioned technical solutions, the silica alumina ratio of preferred technical solution, the molecular sieve is greater than 2.
In the above-mentioned technical solutions, preferred technical solution, also containing including element week in the adsorbent of molecular sieve
At least one of Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element element in phase table.
In the above-mentioned technical solutions, preferred technical solution, the IIth element A is selected from magnesium and calcium in the periodic table of elements
At least one of；Ith B race element is selected from least one of copper, silver；IIIth B race element in lanthanum, cerium, yttrium at least
It is a kind of.
In the above-mentioned technical solutions, preferred technical solution, ZSM type molecular sieve is selected from packet in the adsorbent of molecular sieve
At least one of ZSM-5, ZSM-23, ZSM-11, ZSM-48 are included, wherein the silica alumina ratio of the molecular sieve is greater than 20.
In the above-mentioned technical solutions, preferred technical solution, in treated waste water, the content of BaP is less than 0.03
Ug/L, ammonia-nitrogen content are less than 100mg/L, and COD is less than 2000mg/L and uses nitrogen after the adsorbent of molecular sieve adsorption saturation
It is continued to use after being regenerated 3 ~ 60 hours at 80 ~ 200 DEG C.
In the above-mentioned technical solutions, preferred technical solution, adsorbent bed operation temperature are 10 ~ 80 DEG C, and operating pressure is normal
Pressure.
In the above-mentioned technical solutions, preferred technical solution, be passed through in adsorbent bed air, ozone, in double water oxygen water extremely
Few one kind.
In the above-mentioned technical solutions, preferred technical solution, before waste water feeding is filled with the adsorbent bed of adsorbent, through making a living
Property charcoal pretreatment.
In the above-mentioned technical solutions, preferred technical solution, after the adsorbent of molecular sieve adsorption saturation, again with nitrogen
After life, then with 60-200 DEG C of hot water injection.
In the above-mentioned technical solutions, preferred technical solution, in treated waste water, the content of tar is less than 10mg/L；
After the adsorbent of molecular sieve tar adsorption saturation, continued to use after being regenerated 3 ~ 20 hours with nitrogen at 100 ~ 200 DEG C.
In the above-mentioned technical solutions, preferred technical solution, adsorption tower operation temperature are 10 ~ 60 DEG C, and operating pressure is normal
Pressure.
In the above-mentioned technical solutions, preferred technical solution, be passed through in adsorption tower air, ozone, in double water oxygen water extremely
Few one kind.
In the above-mentioned technical solutions, preferred technical solution is that the exhaust gas after regeneration enters in the pre-cooling tower before desulfurizing tower,
Or before entering coal gas primary cooler.
In the above-mentioned technical solutions, preferred technical solution is that the exhaust gas after regeneration enters the pre-cooling tower before desulfurizing tower
Before, or before entrance coal gas primary cooler, first pass through cooling.
In the above-mentioned technical solutions, preferred technical solution, before distilled ammonia wastewater feeding is filled with the adsorption tower of adsorbent, warp
Cross Activated Carbon Pretreatment.
Using the technical program, oil-containing distilled ammonia wastewater is directly adsorbed with adsorbent, solves oil-containing height in distilled ammonia wastewater,
The technical issues of influencing subsequent biochemical system treatment effect.When distilled ammonia wastewater solid ammonium-salt is 300mg/L(ammonium sulfate, chlorination
Ammonium), volatilization ammonia content is 300mg/L(ammonium hydrogen carbonate, free ammonia), COD(COD) it is 3000 ± 1000 mg/L, and
Containing substances such as phenols, cyanide, oil slick (tar light oil mainly based on aromatic hydrocarbon), temperature is 70 DEG C~90 DEG C, is passed through
After adsorption cleaning, (the NH containing ammonia nitrogen3- N) it is less than 10mg/L, COD is less than 400mg/L.Entire treatment process process is short, and equipment is thrown
Money saves, and regenerative operation is simple and reliable, and low energy consumption, achieves preferable technical effect.
Detailed description of the invention
Fig. 1 is the flow diagram of distilled ammonia wastewater deoiling method of the invention.
I is activated carbon pretreatment system in Fig. 1, and II is adsorption tower, and III is wastewater biochemical pond, and IV is coal gas primary cooler.
The 1 oil-containing distilled ammonia wastewater come for coke-oven plant, 2 be the waste water after Activated Carbon Pretreatment, and 3 be tar adsorption and organic
Waste water after object, ammonia nitrogen, 4 be 50 ~ 400 DEG C of nitrogen, and 5 be 60-200 DEG C of hot water, and 6 be to regenerate the gas come.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[embodiment 1]
Specific embodiment device process as shown in Figure 1,60mg/L containing tar-concentration, the ammonia content containing volatilization are 300mg/L
(ammonium hydrogen carbonate, free ammonia), COD(COD) it is that the distilled ammonia wastewater of 3000 mg/L is sent into the absorption for being filled with adsorbent
Tower, wherein the adsorbent is adsorbent of molecular sieve, adsorbent uses hydrophobic type ZSM 5 molecular sieve；Waste water after absorption
It is sent into tank；A part of waste water in tank is as cooling water reuse, a part discharge.Tar contains in treated waste water
Amount is 1.2 mg/L, and ammonia-nitrogen content 4mg/L, COD content is 300 mg/L.
[embodiment 2]
The distilled ammonia wastewater feeding of specific embodiment device process as shown in Figure 1, the 68mg/L containing tar-concentration is filled with suction
Attached dose of adsorption tower, wherein the adsorbent is adsorbent of molecular sieve, adsorbent uses TS-1 type molecular sieve；Steaming after absorption
Ammonia waste water is sent into tank；A part of waste water in tank is as cooling water reuse, a part discharge.Ammonia still process before processing is useless
Water 68mg/L containing tar-concentration, the ammonia content containing volatilization are 300mg/L, and COD is 3200 mg/L, burnt in treated distilled ammonia wastewater
Oil content is 1.3 mg/L, and ammonia-nitrogen content 4mg/L, COD content is 325 mg/L.
[embodiment 3]
The distilled ammonia wastewater feeding of specific embodiment device process as shown in Figure 1, the 50mg/L containing tar-concentration is filled with suction
Attached dose of adsorption tower, wherein the adsorbent is adsorbent of molecular sieve, adsorbent uses Ti-MOR molecular sieve；Steaming after absorption
Ammonia waste water is sent into tank；A part of waste water in tank is as cooling water reuse, a part discharge.
Distilled ammonia wastewater 50mg/L containing tar-concentration before processing, the ammonia content containing volatilization are 280mg/L, and COD is 3200 mg/
L, in treated distilled ammonia wastewater, tar content is 0.8 mg/L, and ammonia-nitrogen content 4mg/L, COD content is 328 mg/L.
[embodiment 4]
The distilled ammonia wastewater feeding of specific embodiment device process as shown in Figure 1, the 85mg/L containing tar-concentration is filled with suction
Attached dose of adsorption tower, wherein the adsorbent is adsorbent of molecular sieve, adsorbent uses hydrophobic Ti-MWW type molecular sieve；It inhales
Attached distilled ammonia wastewater is sent into biochemistry pool.
Distilled ammonia wastewater 75mg/L containing tar-concentration before processing, the ammonia content containing volatilization are 350mg/L, and COD is 3500 mg/
L, in treated distilled ammonia wastewater, tar content is 0.25 mg/L, and ammonia-nitrogen content 6mg/L, COD content is 330 mg/L.
After adsorbent saturation, with nitrogen regeneration 5 hours of 150 DEG C, the exhaust gas after regeneration entered the first cold tower before desulfurizing tower,
Adsorbent continues to use after regeneration, the distilled ammonia wastewater 60mg/L containing tar-concentration before processing, and the ammonia content containing volatilization is 380mg/L,
COD is 3600 mg/L, and in treated distilled ammonia wastewater, tar content is 0.2 mg/L, ammonia-nitrogen content 5mg/L, COD content
For 320 mg/L, adsorbent activity can be restored.
[embodiment 5]
The distilled ammonia wastewater feeding of specific embodiment device process as shown in Figure 1, the 55mg/L containing tar-concentration is filled with suction
Attached dose of adsorption tower, wherein the adsorbent is adsorbent of molecular sieve, the Y zeolite molecular sieve that adsorbent uses copper modified；It inhales
Attached distilled ammonia wastewater is sent into tank；A part of waste water in tank is as cooling water reuse, a part discharge.After processing
Waste water in tar content be 0.6mg/L.
[embodiment 6]
The distilled ammonia wastewater feeding of specific embodiment device process as shown in Figure 1, the 60mg/L containing tar-concentration is filled with suction
Attached dose of adsorption tower, wherein the adsorbent is adsorbent of molecular sieve, adsorbent uses the ZSM-5 zeolite molecule of copper zinc modification
The silica alumina ratio of sieve, molecular sieve is greater than 600；Distilled ammonia wastewater after absorption is sent into tank；A part of waste water in tank
As cooling water reuse, a part discharge.Tar content is 1.1mg/L in treated waste water.
[embodiment 7]
The distilled ammonia wastewater feeding of specific embodiment device process as shown in Figure 1, the 76mg/L containing tar-concentration is filled with suction
Attached dose of adsorption tower, wherein the adsorbent is adsorbent of molecular sieve, adsorbent uses the ZSM-5 zeolite molecule of copper zinc modification
The silica alumina ratio of sieve, molecular sieve is greater than 600；Air is passed through in adsorption process in adsorption tower, the distilled ammonia wastewater after absorption is sent into
Tank；A part of waste water in tank is as cooling water reuse, a part discharge.BaP content in treated waste water
For 0.8mg/L.
[embodiment 8]
The distilled ammonia wastewater feeding of specific embodiment device process as shown in Figure 1, the 76mg/L containing tar-concentration is filled with suction
Attached dose of adsorption tower, wherein the adsorbent is adsorbent of molecular sieve, adsorbent uses the ZSM-5 zeolite molecule of copper zinc modification
The silica alumina ratio of sieve, molecular sieve is greater than 600；Ozone is passed through in adsorption process in adsorption tower, the waste water after absorption is sent into water storage
Pond；A part of waste water in tank is as cooling water reuse, a part discharge.BaP content is in treated waste water
1.3mg/L。
[embodiment 9]
The distilled ammonia wastewater of the 80mg/L containing tar-concentration is sent into the adsorption tower for being filled with adsorbent, wherein the adsorbent is molecule
Sieve adsorbant, adsorbent use hydrophobic Ti-MWW type molecular sieve；Distilled ammonia wastewater after absorption is sent into biochemistry pool.
Distilled ammonia wastewater 70mg/L containing tar-concentration before processing, the ammonia content containing volatilization are 350mg/L, and COD is 3500 mg/
L, in treated distilled ammonia wastewater, tar content is 0.2 mg/L, and ammonia-nitrogen content 6mg/L, COD content is 300 mg/L.
After adsorbent saturation, with nitrogen regeneration 5 hours of 150 DEG C, the exhaust gas after regeneration entered the pre-cooling tower before desulfurizing tower,
After nitrogen regeneration, then with 90 DEG C of hot water adsorbent is cleaned, adsorbent continues to use after cleaning, and the distilled ammonia wastewater before processing is containing coke
Oil concentration 70mg/L, the ammonia content containing volatilization are 360mg/L, and COD is 3400 mg/L, in treated distilled ammonia wastewater, tar content
For 0.1 mg/L, ammonia-nitrogen content 5mg/L, COD content is 200 mg/ L, and adsorbent activity can be restored.
[embodiment 10]
The distilled ammonia wastewater of the 80mg/L containing tar-concentration is sent into the adsorption tower for being filled with adsorbent, wherein the adsorbent is molecule
Sieve adsorbant, adsorbent use hydrophobic Ti-MWW type molecular sieve；Distilled ammonia wastewater after absorption is sent into biochemistry pool.
Distilled ammonia wastewater 75mg/L containing tar-concentration before processing, the ammonia content containing volatilization are 350g/L, and COD is 3300 mg/L,
In treated distilled ammonia wastewater, tar content is 0.25 mg/L, and ammonia-nitrogen content 5mg/L, COD content is 300 mg/L.
After adsorbent saturation, with nitrogen regeneration 5 hours of 150 DEG C, before the exhaust gas after regeneration enters coal gas primary cooler, nitrogen
After regeneration, then with 90 DEG C of hot water adsorbent is cleaned, adsorbent continues to use after cleaning, and the distilled ammonia wastewater before processing is dense containing tar
75mg/L is spent, the ammonia content containing volatilization is 360mg/L, and COD is 3200 mg/L, and in treated distilled ammonia wastewater, tar content is
0.1 mg/L, ammonia-nitrogen content 5mg/L, COD content are 290 mg/L, and adsorbent activity can be restored.
[embodiment 11]
The distilled ammonia wastewater of the 78mg/L containing tar-concentration is sent into the pretreatment adsorption tower that active carbon is housed, pretreated distilled ammonia wastewater
Into the adsorption tower for being filled with adsorbent, wherein the adsorbent is adsorbent of molecular sieve, adsorbent uses hydrophobic MOR type
Molecular sieve；Distilled ammonia wastewater after absorption is sent into biochemistry pool.
Distilled ammonia wastewater 75mg/L containing tar-concentration before processing, the ammonia content containing volatilization are 350mg/L, and COD is 3500 mg/
L, in treated distilled ammonia wastewater, tar content is 0.1mg/L, and ammonia-nitrogen content 5mg/L, COD content is 240 mg/L.
After adsorbent saturation, with nitrogen regeneration 5 hours of 150 DEG C, before the exhaust gas after regeneration enters coal gas primary cooler, nitrogen
After regeneration, then with 90 DEG C of hot water adsorbent is cleaned, adsorbent continues to use after cleaning, and the distilled ammonia wastewater before processing is dense containing tar
75mg/L is spent, the ammonia content containing volatilization is 350mg/L, and COD is 3500 mg/L, and in treated distilled ammonia wastewater, tar content is
0.1 mg/L, ammonia-nitrogen content 5mg/L, COD content are 200 mg/L, and adsorbent activity can be restored.
Claims (10)
1. a kind of distilled ammonia wastewater removes oil treatment process, comprising the following steps:
A) the oil-containing distilled ammonia wastewater of coke-oven plant is sent into the adsorption tower for being filled with crystallite adsorbent,
B) distilled ammonia wastewater after adsorbing is sent into wastewater biochemical pond,
C) adsorbent after adsorption saturation, with 100 ~ 400 DEG C of nitrogen or steam regeneration.
2. the method for distilled ammonia wastewater oil removing according to claim 1, it is characterised in that the crystallite adsorbent is molecule
Sieve adsorbant, it includes X-type molecular sieve, Y type molecular sieve, A type molecular sieve, TS-1, Ti-MWW, Ti-MOR, ZSM type that molecular sieve, which is selected from,
Molecular sieve, modenite, beta molecular sieve, SAPO type molecular sieve, MCM-22, MCM-49, MCM-56, ZSM-5/ modenite,
ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/ modenite, ZSM-5/Magadiite, ZSM-5/ β zeolite/modenite, ZSM-
5/ β zeolite/at least one of Y zeolite or ZSM-5/Y zeolite/modenite, the silica alumina ratio of the molecular sieve is greater than
2。
3. distilled ammonia wastewater according to claim 1 removes oil treatment process, it is characterised in that the adsorbent of molecular sieve
In also containing including in the periodic table of elements in the Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element
At least one element.
4. distilled ammonia wastewater according to claim 4 removes oil treatment process, it is characterised in that in the periodic table of elements
IIth element A is selected from least one of magnesium and calcium；Ith B race element is selected from least one of copper, silver；The choosing of IIIth B race element
From at least one of lanthanum, cerium, yttrium；In the adsorbent of molecular sieve ZSM type molecular sieve be selected from including ZSM-5, ZSM-23,
At least one of ZSM-11, ZSM-48, ZSM-22, wherein the silica alumina ratio of the molecular sieve is greater than 20.
5. distilled ammonia wastewater according to claim 1 remove oil treatment process, it is characterised in that adsorption tower operation temperature be 10 ~
80 DEG C, operating pressure is normal pressure.
6. distilled ammonia wastewater according to claim 1 removes oil treatment process, it is characterised in that in treated waste water, benzo
For the content of pyrene less than 0.03 ug/L, ammonia-nitrogen content is less than 100mg/L, and COD is less than 2000mg/L, the adsorbent of molecular sieve
After adsorption saturation, continued to use after being regenerated 3 ~ 60 hours with nitrogen at 80 ~ 200 DEG C.
7. distilled ammonia wastewater according to claim 1 removes oil treatment process, it is characterised in that the exhaust gas after regeneration enters de-
In pre-cooling tower before sulphur tower, or before entrance coal gas primary cooler.
8. distilled ammonia wastewater according to claim 6 removes oil treatment process, it is characterised in that the exhaust gas after regeneration enters de-
Before pre-cooling tower before sulphur tower, or before entrance coal gas primary cooler, first pass through cooling.
9. distilled ammonia wastewater according to claim 1 removes oil treatment process, it is characterised in that waste water feeding is filled with absorption
Before the adsorption tower of agent, by Activated Carbon Pretreatment.
10. distilled ammonia wastewater according to claim 6 removes oil treatment process, it is characterised in that the adsorbent of molecular sieve
After adsorption saturation, after nitrogen regeneration, then with 60-200 DEG C of hot water injection.
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