CN101597124B - Method for treating coal gasification wastewater containing phenol and ammonia - Google Patents
Method for treating coal gasification wastewater containing phenol and ammonia Download PDFInfo
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- CN101597124B CN101597124B CN2009100365419A CN200910036541A CN101597124B CN 101597124 B CN101597124 B CN 101597124B CN 2009100365419 A CN2009100365419 A CN 2009100365419A CN 200910036541 A CN200910036541 A CN 200910036541A CN 101597124 B CN101597124 B CN 101597124B
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Abstract
The invention relates to a method for treating coal gasification wastewater containing phenol and ammonia. The method comprises the following steps: single tower alkali injection and pressurization steam stripping removal of acidic gas and ammonia, three-level dephlegmation of lateral line tapped gas, extraction of phenol by diisopropyl ether and solvent recovery. The cold and hot coal gasification wastewater, according to a certain proportion, respectively enters a pressurization single tower from the upper part and middle upper part of a wastewater steam stripping tower, and acid gas is discharged from the tower top; the lateral line withdrawal mixed gas goes through three-level dephlegmation to obtain high-concentration ammonia, alkali is injected at the position below the lateral line to transform fixed ammonia into free ammonia which is to be removed; counter-current extraction is carried out on removed ammonia, residue of acid gas and diisopropyl ether to dephenolize; extraction solvent is recovered by a solvent recovery tower and a solvent steam stripping tower to obtain the byproduct, namely crude phenol. In the method of the invention, the process removing acid gas, free ammonia and fixed ammonia is carried out simultaneously on the coal gasification wastewater in the wastewater steam stripping single tower, as a result, high-concentration ammonia is obtained, the content of carbon dioxide, sulfureted hydrogen, free ammonia and fixed ammonia in tower kettle purified water is extremely low, encrustment is not prone to take place, and the purified coal gasification wastewater meets the requirement of follow-up biochemical treatment.
Description
Technical field
The present invention relates to the method that a kind of processing contains phenol ammonia coal gasification waste water, particularly a kind of method of annotating alkali pressurization stripping depickling simultaneously deamination processing coal gasification waste water.
Background technology
The high pollution waste water that produces when coal gasification waste water comes from gas washing, water quality composition complexity, pollution substance mainly contains ammonia, carbonic acid gas, unit phenol, polyphenol, lipid acid etc., and hydrogen sulfide content is less.These materials all are polar materials, and ammonia, carbonic acid gas and hydrogen sulfide are volatile weak electrolyte in the aqueous solution.H in the waste water
2S, CO
2Deng sour gas cognition treating processes is caused interference, cause equipment corrosion, fouling, and ammonia also has restraining effect to microorganism, influence follow-up biochemical treatment.For such waste water, the mode that generally adopts the chemical separating flow process to combine with biochemical treatment is handled both at home and abroad.The existing chemical separating treatment scheme of coal gasification waste water generally comprises unit such as depickling, extraction, deamination, solvent recuperation, to remove sour gas, reclaims phenol, ammonia etc.Waste water is removed tar and part light oil after pre-treatment such as flash distillation, sedimentation, enter extracting tower to remove CO
2, H
2Sour gas such as S enter the extraction tower extracting and dephenolizing then.Waste water after the extraction enters biochemical treatment workshop section again and carries out biochemical treatment after deamination and solvent recuperation.
The most outstanding shortcoming of existing technology has: water quality is alkalescence and is unfavorable for extraction during extraction, thereby causes dephenolization effect bad; Because the carbon dioxide content height, and deamination in the end carries out, so the situation of more carbonic acid gas and ammonia coexistence is arranged in the operational process always, both react and produce the crystallization of ammonia salt, thereby cause equipment scaling, stop up seriously, influence plant efficiency; Existing technology belongs to foaming system, and liquid flooding easily takes place, and the equipment that influences normally moves.
Single tower pressurization stripping is that commercial runs such as refining of petroleum, petrochemical complex produce one of effective treatment process of sour water.U.S. Pat 3518167 and Chinese invention patent 90107237.0,98114341.5 all disclose single tower stripping side line and have extracted the method for handling sour water out, by the stripping tower top hydrogen sulfide of purifying, the middle part of the tower ammonia of purifying, hydrogen sulfide and the ammonia in the stripping sewage is come in the bottom of tower.Chinese invention patent application 200710053952.X discloses a kind of processing sulfide hydrogen and propylhomoserin sewage technology, is primarily aimed at sulfide hydrogen and ammonia total concn greater than the 50000mg/L occasion.Chinese invention patent application 200610036072.7 discloses the method and apparatus that a kind of single tower pressurization stripping is handled coal gasification wastewater, take stripping depickling deamination, extracting and dephenolizing and three steps of solvent recuperation at coal gasification waste water, improve the decreasing ratio of carbonic acid gas and ammonia, thereby the pH value that reduces extraction is improved dephenolization effect, but this method does not take into full account the existence of fixed ammonia.Contain thiocyanate, thiosulfate anion, nitrate radical, nitrite anions, sulfate radical, cyanogen root, inferior sulfate radical and other fatty acid materials in the coal gasification waste water, easy and ammonia root forms fixed ammonia.This patented technology can not be removed fixed ammonia, and the middle fixed ammonia content of purifying waste water that single tower comes out surpasses the water quality standard of follow-up biochemical treatment, influences biochemical treatment.
Summary of the invention
The objective of the invention is to defective, provide a kind of processing of removing fixed ammonia and dephenolize simultaneously to contain the method for phenol ammonia coal gasification waste water at prior art.
Purpose of the present invention is achieved through the following technical solutions:
A kind of processing contains the method for phenol ammonia coal gasification waste water, comprises the steps:
(1) (1) single tower alkali injection pressurization stripping depickling deamination: the coal gasification waste water of carbonated, ammonia and phenol is divided into two bursts of chargings enters the sewage stripping tower, wherein one raw water is through being cooled to the packing section top that enters sewage stripping tower cat head after 30～50 ℃ as cold feed, tower top pressure is 0.2～0.6MPa, 40～80 ℃ of temperature; Another strand raw water is hot feed, after extracting gas heat exchange to 130～155 ℃ out with side line, enters the first layer tower tray under the sewage stripping tower packing section as hot feed; The cold feed of described raw water and hot feed weight ratio are 0.1～1: 1; Cold feed is joined with hot feed after absorbing ammonia, carry out heat exchange at steam with the rising of tower still, ammonia, carbonic acid gas and hydrogen sulfide stripping are come out, 3～15 column plate positions are that 20～60% caustic-soda aqueous solutions pressurization back is injected in the stripping Tata with mass percent concentration below side line, fixed ammonia is converted into ammonia removes; Caustic-soda aqueous solution is 2～4: 1000 with the weight ratio that contains phenol ammonia coal gasification waste water; Discharge gas mixture from single column overhead and discharge from sewage stripping tower cat head after the cooling phase-splitting, get the high density ammonia from single tower side line extraction gas mixture through three grades of fractional condensation, lime set is returned head tank; Tower bottom pressure is 0.35～0.65MPa, 120～170 ℃ of temperature; Extraction still liquid pH value is 5～7 at the bottom of the tower;
(2) extracting and dephenolizing: the still liquid of step (1) extraction is that counter-current extraction is carried out on the extraction tower top of extraction agent through being cooled to send into after 40～60 ℃ with the diisopropyl ether, and the volume ratio of diisopropyl ether and sewage is 1: 5～10; The extracting phase of extraction tower bottom extraction is delivered to the solvent stripping tower, and making tower top pressure is 0.1～0.2MPa, and temperature is 60～100 ℃, is 0.1～0.2MPa at the bottom of the tower, and temperature is 100～120 ℃, and extraction still liquid send follow-up biochemical treatment at the bottom of the tower.
For further realizing the object of the invention, described step (2) extracting and dephenolizing also comprises solvent recuperation, be that the extraction phase of extraction tower cat head extraction is delivered to solvent recovery tower, making tower top pressure is 0.1～0.2MPa, and temperature is 55～120 ℃, is 0.1～0.2MPa at the bottom of the tower, temperature is 200～220 ℃, reflux ratio 0.2～0.6, from cat head extraction diisopropyl ether loopback solvent tank recycling, extraction product crude phenols at the bottom of the tower; From solvent stripping tower cat head extraction diisopropyl ether loopback solvent tank, for recycling.
The gas mixture weight of described side line extraction accounts for 8～15% of cold and hot raw water weight.
Three grades of fractional condensation are to produce gas ammonia by three grades of alternating temperature transformations, wherein, the working pressure of one-level partial condenser is 0.4～0.5MPa, service temperature is 110～150 ℃, the working pressure of secondary partial condenser is 0.35～0.4MPa, service temperature is 70～115 ℃, and the working pressure of three grades of partial condensers is 0.2～0.35MPa, and service temperature is 30～50 ℃.
The present invention compared with prior art has following advantage:
(1) the inventive method is compared Chinese patent 200610036072.7, and the fixed ammonia content by in the method effective elimination sewage of annotating alkali satisfies follow-up biochemical processing requirements.
(2) the chemical industry treatment process that generally adopts of the relative gasification industry of the inventive method realizes depickling and deamination in a tower, is about to extracting tower and deammoniation tower and is kept to a single tower, has reduced facility investment and working cost.
(3) the chemical industry treatment process that generally adopts of the relative gasification industry of the inventive method has improved CO
2With the decreasing ratio of ammonia, total ammonia content is reduced to 300mgL
-1Below, thereby alleviate crystallization of ammonia salt and scale problems in original flow process.
(4) employing of the inventive method makes the tower still pH value of purifying waste water be reduced to 5～7, be slant acidity, thereby improve extraction solvent dephenolization effect subsequently greatly, the pollution load of processed waste water descends significantly, alleviate the processing load of biochemical section, solve the improvement difficult problem of high-concentration phenolic wastewater.
(5) stripping tower 1 adopts pressurizing tower, suppresses coal gasification waste water water quality system foaming problem effectively, guarantees the long-term stability operation of equipment.
Description of drawings
Fig. 1 is a wastewater treatment equipment synoptic diagram of the present invention.
Embodiment
Below in conjunction with the drawings and specific embodiments the present invention is further described, the present invention is not limited to this.
It is similar substantially that the present invention handles the device of 200610036072.7 1 kinds of single towers pressurization strippings processing coal gasification wastewaters of Chinese invention patent application that the device contain phenol ammonia coal gasification waste water and applicant propose.Mainly be to have increased caustic-soda aqueous solution to annotate feeder apparatus and dephenolize device.As shown in Figure 1, the sewage stripping tower 1 that the present invention handles the device that contains phenol ammonia coal gasification waste water is divided into three sections, and top is packing section, middle part and bottom are the tower tray section, and cat head to hot charge water inlet is a packing section, and random packing is housed, be used for ammonia and absorb, be the sour gas rectifying section; Hot charge water inlet to side line ammonia gas mixture extraction mouth is a middle part tower tray section, is used for strippings such as carbonic acid gas, is the sour gas stripping stage; Side line ammonia gas mixture is adopted and is exported at the bottom of the tower is bottom tower tray section, is used for the ammonia stripping, is the ammonia stripping stage.Three sections tower diameter ratio is 0.2～0.8: 0.5～1: 1.Feed pipe is connected with water pump.Water pump is connected with hot inlet channel 12 with cold inlet channel 11 respectively, cold inlet channel 11 and hot inlet channel 12 connect sewage stripping tower 1, the cat head of sewage stripping tower 1 connects fractional condensation jar 9, the gaseous phase outlet emptying of fractional condensation jar 9 or to incinerator, the liquid phase of fractional condensation jar 9 exports back head tank.The side line of sewage stripping tower 1 connects one-level partial condenser 5, one-level partial condenser 5 is connected with secondary partial condenser 6 again, secondary partial condenser 6 is connected with three grades of partial condensers 7 again, one-level partial condenser 5, secondary partial condenser 6 and three grades of partial condensers 7 constitute three grades of partial condensers, its liquid phase outlet is connected with head tank by pipeline respectively, and the gaseous phase outlet of three grades of partial condensers 7 connects follow-up ammonia refining plant.The tower still of sewage stripping tower 1 adds thermal recovery reboiler and straight-through vapor phase bonded mode, and promptly the bottom steam pipeline at sewage stripping tower 1 is connected with reboiler respectively with at the bottom of the sewage stripping Tata, and reboiler is connected with sewage stripping tower bottom tower tray section.
Connect extraction tower 2 at the bottom of the tower of sewage stripping tower 1, extraction tower 2 cats head connect solvent recovery tower 4, and solvent recovery tower 4 cats head connect solvent tank 8, connect the crude phenols retrieving arrangement at the bottom of solvent recovery tower 4 towers; Connect solvent stripping tower 3 at the bottom of extraction tower 2 towers, solvent stripping tower 3 cats head connect solvent tank 8, adhesion processing at the bottom of solvent stripping tower 3 towers; Solvent tank 8 connects at the bottom of the tower of extraction tower 2.
Following 3～15 blocks of column plates of the side line of sewage stripping tower 1 are provided with the alkali lye import, are connected with lye pump 13 by pipeline.
During use, as shown in Figure 1, contain phenol, ammonia, CO
2, H
210 fens hot and cold two stocks of the coal gasification waste water of pollutents such as S do not enter sewage stripping tower 1 from top and middle and upper part, and raw water cold feed and hot feed weight ratio are 0.1～1: 1.The sewage stripping tower absorbs water coolant with cold raw water as cat head.Owing to exist in the waste water and negatively charged ion bonded fixed ammonias such as CN-, SCN-, Cl-, under existing Heating temperature, can't decompose, therefore be that 20～60% caustic-soda aqueous solution enters sewage stripping tower 1 by lye pump 13 from 3～15 blocks of column plates below the side line with mass percent concentration, caustic-soda aqueous solution mixes with cold and hot waste water, thereby being converted into free ammonia, fixed ammonia removes, for example reactional equation: NaOH+NH
4CN===NaCN+NH
3+ H
2O; The CO that stripping goes out
2, H
2Sour gas such as S and little ammonia, light oil, water vapor 14 through 9 fractional condensation of fractional condensation jars after, sour gas 17 is discharged from fractional condensation jar 9 tops, directly emptying or advance torch and burn 18 times head tanks of the liquid phase of fractional condensation jar 9.Enter one-level partial condenser 5, secondary partial condenser 6 and three grades of partial condensers 7 successively from the gas mixture 15 of sewage stripping tower 1 side line extraction, carry out three grades of fractional condensation, the 20 times head tanks of lime set that contain portion water and little ammonia, the gas phase part 19 of three grades of partial condensers 7 enter the refining workshop section of ammonia and are processed into liquefied ammonia.The weight that side line is extracted gas mixture 15 out accounts for 8～15% of cold and hot raw water weight.Extracting out in the gas mainly is water vapour and ammonia, and the position of extraction is the higher tower position of ammonia concentration, and the extraction amount is along with the total amount of cold and hot charging increases and increases, and the ratio of extracting out is also relevant with energy.The extraction amount is excessive, and the most heats that provide at the bottom of the tower have all rung off from side line, will not have enough heats that sour gas in the hot feed and ammonia are evaporated.Enter extraction tower 2 tops after sewage stripping tower bottoms 16 behind acid gas removal and the ammonia is cooled to 30～60 ℃, carry out counter-current extraction with diisopropyl ether.Extraction phase 21 pumps in the solvent recovery tower 4, and the tower still gets crude phenols 23, and the diisopropyl ether 25 that the solvent recuperation column overhead is come out is recycled to solvent tank 8 for recycling.The diisopropyl ether of solvent tank 8 mainly comes from the diisopropyl ether that diisopropyl ether 25 that fresh diisopropyl ether solvent 25, solvent stripping tower cat head come out and solvent recuperation column overhead are come out.The surplus phase 22 of the extraction of extraction tower 2 pumps in the solvent stripping tower 3, delivers to solvent tank 8 for recycling from the diisopropyl ether 25 of solvent stripping tower cat head extraction, and extraction still liquid 24 send follow-up biochemical treatment at the bottom of the tower.Regularly in solvent tank 8, replenish the fresh solvent diisopropyl ether, supply diisopropyl ether to extraction tower 2 by solvent tank 8.
Embodiment 1～3rd, adopts the case study on implementation of patented technology of the present invention, and embodiment 4 is the Comparative Examples that adopt the technology implementation of Chinese patent 200610036072.7.
Embodiment 1
The device that the above-mentioned processing of this example application contains phenol ammonia coal gasification waste water carries out wastewater treatment.The coal gasification wastewater total phenol content is 6010mgL
-1, free ammonia 12.61gL
-1, fixed ammonia 0.60gL
-1, CO
24.26gL
-1, the pH value is 9.8,87 ℃ of water temperatures, and 92.64 tons/hour of flows are handled by flow process shown in Figure 1.The hot and cold charge ratio of sewage stripping tower is 1: 3.6, and tower top temperature is 45.86 ℃, and tower top pressure is 0.47MPa, and column bottom temperature is 157 ℃, and tower bottom pressure is 0.47MPa, and mass percent concentration is that 20% caustic-soda aqueous solution flow is 380kghr
-1, side line extraction temperature is 140.0 ℃, pressure 0.46MPa.The working pressure of one-level partial condenser is 0.40MPa in three grades of fractional condensation, and service temperature is 137.7 ℃, and the working pressure of secondary partial condenser is 0.36MPa, and service temperature is 79.9 ℃, and the working pressure of three grades of partial condensers is 0.34MPa, and service temperature is 37.3 ℃.Extraction tower adopts packing tower, and solvent sewage volume ratio is 1: 10, solvent stripping tower tower top pressure 0.11MPa, produced quantity 2600kgh
-1, 55 ℃ of condensing temperatures, tower bottom pressure 0.12MPa, 102 ℃ of temperature.Solvent recovery tower tower top pressure 0.11MPa, 110 ℃ of temperature, tower bottom pressure 0.12MPa, 215 ℃ of temperature, reflux ratio 0.5.Total phenol content 280mgL in the waste water after the processing
-1, free ammonia 30mgL
-1, fixed ammonia 200mgL
-1Ammonia level is 93% in the refining rich ammonia of gas phase part 19 deammoniations of three grades of partial condensers 7, the carbonic acid gas trace, and hydrogen sulfide does not detect.
Embodiment 2
The device that the above-mentioned processing of this example application contains phenol ammonia coal gasification waste water carries out wastewater treatment.The coal gasification wastewater total phenol content is 6050mgL
-1, free ammonia 20.43gL
-1, fixed ammonia 1.34gL
-1, CO
22.83gL
-1, the pH value is 11.0,89 ℃ of water temperatures, and 60.01 tons/hour of flows are handled by flow process shown in Figure 1.The cold and hot charge ratio of sewage stripping tower is 1: 4.0,41.14 ℃ of tower top temperatures, tower top pressure 0.48MPa, 161.7 ℃ of column bottom temperatures, tower bottom pressure 0.51MPa, 60% (quality) alkali lye 120kghr
-1, 151.0 ℃ of side line extraction temperature, pressure 0.49MPa.The working pressure of three grades of fractional condensation one-level partial condensers is 0.40MPa, and service temperature is 144.8 ℃, and the working pressure of secondary partial condenser is 0.36MPa, and service temperature is 97.2 ℃, and the working pressure of three grades of partial condensers is 0.20MPa, and service temperature is 41.35 ℃.Extraction tower adopts packing tower, and solvent sewage volume ratio is 1: 6, solvent stripping tower tower top pressure 0.12MPa, produced quantity 2500kgh
-1, 50 ℃ of condensing temperatures, tower bottom pressure 0.13MPa, 102.2 ℃ of temperature.Solvent recovery tower tower top pressure 0.11MPa, 110 ℃ of temperature, tower bottom pressure 0.12MPa, 215 ℃ of temperature, reflux ratio 0.3.Total phenol content 299mgL in the waste water after the processing
-1, free ammonia 50mgL
-1, fixed ammonia 220mgL
-1Ammonia level is 92% in the refining rich ammonia of gas phase part 19 deammoniations of three grades of partial condensers 7, the carbonic acid gas trace, and hydrogen sulfide does not detect.
Embodiment 3
The device that the above-mentioned processing of this example application contains phenol ammonia coal gasification waste water carries out wastewater treatment.The coal gasification wastewater total phenol content is 5415.9mgL
-1, free ammonia 19.66gL
-1, fixed ammonia 0.37gL
-1, CO
23.94gL
-1, the pH value is 10.5,85 ℃ of water temperatures, and 85.4 tons/hour of flows are handled by flow process shown in Figure 1.The cold and hot charge ratio of sewage stripping tower is 1: 3,40.6 ℃ of tower top temperatures, tower top pressure 0.50MPa, 165 ℃ of column bottom temperatures, tower bottom pressure 0.52MPa, 20% (quality) alkali lye 350kghr
-1, 152.0 ℃ of side line extraction temperature, pressure 0.50MPa.The working pressure of three grades of fractional condensation one-level partial condensers is 0.42MPa, and service temperature is 145 ℃, and the working pressure of secondary partial condenser is 0.39MPa, and service temperature is 79.69 ℃, and the working pressure of three grades of partial condensers is 0.35MPa, and service temperature is 27.9 ℃.Extraction tower adopts packing tower, and solvent sewage volume ratio is 1: 8, solvent stripping tower tower top pressure 0.11MPa, produced quantity 2600kgh
-1, 52 ℃ of condensing temperatures, tower bottom pressure 0.12MPa, 101.8 ℃ of temperature.Solvent recovery tower tower top pressure 0.11MPa, 112.3 ℃ of temperature, tower bottom pressure 0.12MPa, 212 ℃ of temperature, reflux ratio 0.6.Total phenol content 232mgL in the waste water after the processing
-1, free ammonia 40mgL
-1, fixed ammonia 170mgL
-1Ammonia level is 95% in the refining rich ammonia of gas phase part 19 deammoniations of three grades of partial condensers 7, the carbonic acid gas trace, and hydrogen sulfide does not detect.
Embodiment 4
The coal gasification wastewater total phenol content is 5242.7mgL
-1, free ammonia 9.92gL
-1, fixed ammonia 0.69gL
-1, CO
23.42gL
-1, the pH value is 9.69,90 ℃ of water temperatures, and 81.5 tons/hour of flows are handled by flow process shown in Figure 1.The cold and hot charge ratio of sewage stripping tower is 1: 4,40.6 ℃ of tower top temperatures, tower top pressure 0.47MPa, 157.1 ℃ of column bottom temperatures, tower bottom pressure 0.49MPa, 151.1 ℃ of side line extraction temperature, pressure 0.48MPa.The working pressure of three grades of fractional condensation one-level partial condensers is 0.40MPa, and service temperature is 127.2 ℃, and the working pressure of secondary partial condenser is 0.35MPa, and service temperature is 76.5 ℃, and the working pressure of three grades of partial condensers is 0.31MPa, and service temperature is 38.2 ℃.Extraction tower adopts packing tower, and solvent sewage volume ratio is 1: 10, solvent stripping tower tower top pressure 0.11MPa, produced quantity 2710kgh
-1, 55 ℃ of condensing temperatures, tower bottom pressure 0.12MPa, 102 ℃ of temperature.Solvent recovery tower tower top pressure 0.11MPa, 110 ℃ of temperature, tower bottom pressure 0.12MPa, 215 ℃ of temperature, reflux ratio 0.4.Total phenol content is 220mgL in the waste water after the processing
-1, free ammonia 40mgL
-1, fixed ammonia 650mgL
-1Ammonia level is 92% in the refining rich ammonia of gas phase part 19 deammoniations of three grades of partial condensers 7, the carbonic acid gas trace, and hydrogen sulfide does not detect.
By comparative example 1～3 with do not add embodiment 4 that alkali adopts Chinese patent 200610036072.7 as can be seen, embodiment 1～3, fixed ammonia in the waste water after the processing/ammonia concentration is less than 220mgL
-1, and embodiment 4 fixed ammonias are 650mgL
-1, visible fixed ammonia of the present invention can access good removing, the fixed ammonia effective elimination can be satisfied the follow-up 300mgL of being lower than substantially by the caustic soda amount that uses
-1The biochemical treatment requirement.
Claims (3)
1. a processing contains the method for phenol ammonia coal gasification waste water, it is characterized in that comprising the steps:
(1) single tower alkali injection pressurization stripping depickling deamination: the coal gasification waste water of carbonated, ammonia and phenol is divided into two bursts of chargings enters the sewage stripping tower, wherein one raw water is through being cooled to the packing section top that enters sewage stripping tower cat head after 30～50 ℃ as cold feed, tower top pressure is 0.2～0.6MPa, 40～80 ℃ of temperature; Another strand raw water is hot feed, after extracting gas heat exchange to 130～155 ℃ out with side line, enters the first layer tower tray under the sewage stripping tower packing section as hot feed; The cold feed of described raw water and hot feed weight ratio are 0.1～1: 1; Cold feed is joined with hot feed after absorbing ammonia, carry out heat exchange at steam with the rising of tower still, ammonia, carbonic acid gas and hydrogen sulfide stripping are come out, 3～15 column plate positions are that 20～60% caustic-soda aqueous solutions pressurization back is injected in the sewage stripping Tata with mass percent concentration below side line, fixed ammonia is converted into ammonia removes; Caustic-soda aqueous solution is 2～4: 1000 with the weight ratio that contains phenol ammonia coal gasification waste water; Discharge gas mixture from sewage stripping tower cat head and discharge from sewage stripping tower cat head after the cooling phase-splitting, get the high density ammonia from sewage stripping tower side line extraction gas mixture through three grades of fractional condensation, lime set is returned head tank; Sewage stripping tower tower bottom pressure is 0.35～0.65MPa, 120～170 ℃ of temperature; Extraction still liquid pH value is 5～7 at the bottom of the sewage stripping Tata;
Described three grades of fractional condensation are to produce gas ammonia by three grades of alternating temperature transformations, wherein, the working pressure of one-level partial condenser is 0.4～0.5MPa, service temperature is 110～150 ℃, the working pressure of secondary partial condenser is 0.35～0.4MPa, service temperature is 70～97.2 ℃, and the working pressure of three grades of partial condensers is 0.2～0.35MPa, and service temperature is 30～50 ℃;
(2) extracting and dephenolizing: the still liquid of step (1) sewage stripping tower extraction is that counter-current extraction is carried out on the extraction tower top of extraction agent through being cooled to send into after 40～60 ℃ with the diisopropyl ether, and the volume ratio of diisopropyl ether and sewage is 1: 5～10; The extracting phase of extraction tower bottom extraction is delivered to the solvent stripping tower, making solvent stripping tower tower top pressure is 0.1～0.2MPa, and temperature is 60～100 ℃, and solvent stripping tower tower bottom pressure is 0.1～0.2MPa, temperature is 100～120 ℃, and extraction still liquid send follow-up biochemical treatment at the bottom of the solvent stripping Tata.
2. method according to claim 1, it is characterized in that: described step (2) extracting and dephenolizing also comprises solvent recuperation, solvent recuperation is that the extraction phase of extraction tower cat head extraction is delivered to solvent recovery tower, making the solvent recovery tower tower top pressure is 0.1～0.2MPa, temperature is 55～120 ℃, the solvent recovery tower tower bottom pressure is 0.1～0.2MPa, temperature is 200～220 ℃, reflux ratio 0.2～0.6, from solvent recuperation column overhead extraction diisopropyl ether loopback solvent tank recycling, extraction product crude phenols at the bottom of the solvent recuperation Tata; From solvent stripping tower cat head extraction diisopropyl ether loopback solvent tank, for recycling.
3. method according to claim 1 is characterized in that the gas mixture weight of described side line extraction accounts for 8～15% of cold and hot raw water weight.
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