CN104787954A - Wastewater pretreatment technology - Google Patents
Wastewater pretreatment technology Download PDFInfo
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- CN104787954A CN104787954A CN201510162109.XA CN201510162109A CN104787954A CN 104787954 A CN104787954 A CN 104787954A CN 201510162109 A CN201510162109 A CN 201510162109A CN 104787954 A CN104787954 A CN 104787954A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a wastewater pretreatment technology. Equipment required by the technology comprises a deacidification tower, a deamination tower, a primary feedstock preheater, a secondary feedstock preheater, a dephlegmator, a condensate cooler, a stillage residue cooler, a deacidification tower reboiler, a deamination tower reboiler, an ammonia water buffer tank, an ammonia water tank, an alkaline liquor tank, a feedstock pump and an alkaline adding pump, wherein both the deacidification tower and the deamination tower are rectifying towers; the flow ratio of cold feedstock and hot feedstock of the deacidification tower is 0.1-0.4, the temperature of a stillage residue flowing out of the deamination tower is 134.5 DEG C-138 DEG C, and the temperature of the stillage residue flowing out of the deacidification tower is 155 DEG C-160 DEG C.
Description
Technical field
The present invention relates to a kind of to the pretreatment process containing high-sulfur compound, high ammonia nitrogen, high-COD waste water.
Background technology
It is one of the basic technology of Coal Chemical Industry that crude benzole hydrogenation is refined, and crude benzol, by after further processing and refining, can obtain as multiple products such as pure benzene,toluene,xylene and heavy benzols.Because oil price sharp rises in recent years, compared with taking oil as the petroleum benzene of raw material production, coking benzene has very large profit margin, and therefore crude benzole hydrogenation technique is used widely.And in this technique when removing the various impurity based on thiophene, the sulfide in crude benzol converts hydrogen sulfide to, and nitride transformation becomes ammonia, oxygenate conversion Cheng Shui, thereby produce a kind of waste water containing high-sulfur compound, high ammonia nitrogen, high COD.Although the generation of waste water is little, and the singularity that it has, directly cannot carry out standard biochemical methods process, need to carry out pre-treatment, in prior art, high-sulfur compound, high ammonia nitrogen, high-COD waste water waste water be carried out to pretreated method and mainly contains following several
Chinese patent CN201310202681.5 discloses one (1) and pass into chlorine slowly in the constant-temperature enclosed reactor that high-sulfur compound, high salinity, high-COD waste water be housed, then through passing into hydrogen chloride gas desalination, although the final result process of sulfide, but pass into chlorine can produce hypochlorite and pollute the environment equally, and need to consume the materials such as a large amount of chlorine, cost is higher, and the ammonium chloride of ammonia nitrogen by-product is worth not high, causes whole process economy also poor.
China's document---submarine discharge double tower process flowsheeting is analyzed and is used and can improve (Wei Zhiqiang etc., refining of petroleum and chemical industry, in April, 2012) in disclose flow process with double tower stripping removal of ammonia and nitrogen and sulphur, the document discloses and adopt the process of double tower stripping process containing the waste water of ammonia nitrogen, sulfide, be divided into H by whole stripping treatment process
2s stripping and NH
3stripping, but in the document, handling object is refinery water, and its ammonia-nitrogen content is generally no more than 5000ppm, and sulfide content is generally no more than 10000ppm, for benzene hydrogenation produce sulfide amount at 20000-50000PPm, containing the waste water of ammonia nitrogen amount at 15000-30000ppm, the open technique of the document cannot process, and in the publication, the cold feed ratio of waste water is only about 0.02, and point out in the publication, when cold feed ratio is below 0.015, along with this ratio promotes H
2in S stripper overhead, NH3 content declines gradually, and when cold feed ratio is more than 0.015, continuing to improve this ratio does not have further effect to separation two kinds of pollutents, and energy consumption can be caused on the contrary to increase.And eliminate H through improvement in document
2nH is contained at the bottom of S gas tower hot feed sewage and tower
3sewage heat change, increases NH3 stripper overhead gas, two tower reboiler steam condensed water and H
2s stripping tower charging sewage heat change.Energy-conservation ratio is very large on the surface, but according to law of conservation of energy, the energy-conservation of this place will inevitably be embodied in otherwise power consumption, mentions and utilize steam condenses to carry out heat exchange as thermal source and hot feed in the document, thus improves hot feed temperature, decreases H
2the steam consumption of S stripping tower, but the document does not consider that the vapor condenses water temp after heat exchange reduces again, and the energy that will inevitably consume when it is vaporized again that boiler provides.Therefore provide a kind of and can process the high-sulfur of benzene hydrogenation generation, the double tower stripping process of high ammonia-nitrogen wastewater becomes in prior art the problem needing solution
Summary of the invention
The problem that current existing high-sulfur high ammonia-nitrogen wastewater is difficult to effectively in order to solve, low cost movement also directly enters biochemical treatment, the invention provides a kind of double tower treatment of wastewater from stripping pretreatment technology, this technique is particularly useful for the producer producing high-sulfur compound, high ammonia nitrogen, high-COD waste water in production process.
The invention provides a kind of pretreatment technology of waste water, the equipment that described technique needs comprises extracting tower, deammoniation tower, one-level feed preheater, secondary raw materials preheater, dephlegmator, condensate cooler, still liquid water cooler, extracting tower reboiler, deammoniation tower reboiler, ammoniacal liquor surge tank, ammonia vessel, lye vat, feedstock pump, adds alkali pump, and described extracting tower, deammoniation tower are rectifying tower
The operating process of described technique is as follows
1), temperature is that the raw material waste water of 25-30 DEG C is after feedstock pump, be divided into cold, heat two bursts of chargings, one-level feed preheater is entered by one-level feed preheater material inlet as one of hot feed, 65-70 DEG C is warming up to after the deamination tower bottoms entered with the deamination tower bottoms import of one-level feed preheater carries out a heat exchange, raw material waste water enters secondary raw materials preheater through secondary raw materials preheater material inlet after being flowed out by one-level feed preheater material outlet after a heat exchange, and carry out secondary heat exchange with the depickling tower bottoms that the depickling tower bottoms import by secondary raw materials preheater enters, 105-110 DEG C is increased to by the raw material wastewater temperature of the outflow of secondary raw materials preheater material outlet after secondary heat exchange, then extracting tower is entered as hot feed by the hot feed mouth of extracting tower, raw material waste water as cold feed directly enters extracting tower by tower top by the cold feed mouth being positioned at extracting tower tower top, and raw material waste water flows from top to bottom in extracting tower, under the stripping effect that depickling tower bottom reboiler provides thermal source to produce, be rich in H
2the sour gas of S composition is sent to other workshop sections from extracting tower overhead gas outlet extraction,
2) the depickling tower bottoms being exported out by depickling tower bottoms is exporting from the depickling tower bottoms of secondary raw materials preheater after being cooled to after carrying out heat exchange with raw material waste water wherein flowing out through secondary raw materials preheater, deammoniation tower is entered by deammoniation tower import with self-pressure, deammoniation tower import is equivalent to the 20-30% of the total stage number of deammoniation tower apart from head tray number, meanwhile add by adding the alkali lye stored in the lye vat of alkali pump extraction, this alkali lye enters deammoniation tower through adding alkali mouth, add alkali mouth and deammoniation tower import is positioned at above same column plate, under the stripping effect that deamination tower bottom reboiler provides thermal source to produce, rich ammonia gas is from overhead extraction, dephlegmator cooling rear section gas through being positioned at deammoniation tower tower top becomes liquid phase, as backflow, all the other rich ammonia gas enter condensate cooler through dephlegmator pneumatic outlet by condensate cooler import, after circulating water, condensation becomes liquid phase, described liquid phase enters ammoniacal liquor surge tank through the import of ammoniacal liquor dashpot ammoniacal liquor after exporting outflow by condensate cooler ammoniacal liquor, is then exported to flow into by ammoniacal liquor dashpot ammoniacal liquor to flow into ammonia vessel as product ammoniacal liquor,
The non-condensable gas in condensate cooler condensation process in rich ammonia gas enters ammoniacal liquor surge tank by the non-condensable gas entrance of ammoniacal liquor surge tank, and is exported by the non-condensable gas of ammoniacal liquor surge tank together with the non-condensable gas of discharging with the venting port of ammonia vessel and enter other workshop sections,
The waste water eventually passing through deammoniation tower process enters one-level feed preheater through the outlet of deamination tower bottoms by the import of deamination tower bottoms, with raw material waste water after first time heat exchange, after the deamination tower bottoms outlet of one-level feed preheater is flowed out, enter deamination tower reactor liquid cooling but device by the import of deamination tower bottoms, after circulating water is to 30-35 DEG C, enters other workshop sections by the outlet of deamination tower bottoms;
The throughput ratio of the hot and cold charging of described extracting tower is 0.1-0.4, and described deammoniation tower tower bottoms tower exit temperature is 134.5-138 DEG C, and described extracting tower tower bottoms temperature tower exit temperature is 155-160 DEG C.
Described technique, is characterized in that the throughput ratio of the hot and cold charging of extracting tower is 0.1-0.2.
Described technique, is characterized in that described deammoniation tower, extracting tower adopt the plate distillation column of application film spray no-back mixing column plate
Described technique, is characterized in that described deammoniation tower, extracting tower all adopts stripping tower, preferably adopts the panel type steam stripper of application film spray no-back mixing column plate.
Described film spray no-back mixing column plate is as described in CN200920095625.5.
Described technique, it is characterized in that described high-sulfur compound, the sulfide content of high ammonia-nitrogen wastewater is 20000-50000ppm, ammonia-nitrogen content is 15000-30000ppm, and the waste water sulfide amount eventually passing through deammoniation tower process is down to below 50ppm, and ammonia-nitrogen content is down to below 150ppm.
The beneficial effect that the pretreatment technology of high sulfur-bearing provided by the invention, high ammonia-nitrogen wastewater produces is as follows;
1) by improving existing sewage double tower stripping process sulfur-bearing, nitrogen-containing wastewater technique, improve the throughput ratio of hot and cold charging, unexpected discovery, when adopting the throughput ratio of higher hot and cold charging, can realize the effective elimination to hydrogen sulfide;
2) by reducing the working pressure of extracting tower (under control tower reactor liquid temp is 155-160 DEG C of situation, working pressure is less than 0.6Mpa, both the heat energy consumption of whole technique had been reduced, well removing of ammonia nitrogen can be realized again, in addition utilize the pressure reduction of extracting tower and deammoniation tower, the self-pressure charging of deammoniation tower can be realized.
3) by adopting dephlegmator to replace flash distillation, condensation, both simplified operation, again reducing deammoniation tower integral back-flow ratio, the ammoniacal liquor of deammoniation tower direct production 15-20% can also be controlled, improve the utility value of production efficiency and product.
To sum up, after deammoniation tower, the sulphur content in waste water and ammonia-nitrogen content are all reduced to the level can carrying out biochemical treatment.Overcoming existing double tower stripping process, cannot to process sulfide content be 20000-50000ppm, and ammonia-nitrogen content is the high sulfur-bearing of 15000-30000ppm, the problem of high ammonia-nitrogen wastewater.
Accompanying drawing explanation
Fig. 1 is the process flow diagram to wastewater preprocessing process provided by the invention;
In figure: 1. extracting tower, 101. cold feed mouths, 102. hot feed mouths, 103. extracting tower overhead gas outlets, 104. depickling tower bottoms outlets, 8. extracting tower reboiler;
2. deammoniation tower, 201. deammoniation tower imports, 202. add alkali mouth, 203. deamination tower bottoms outlets, 5. dephlegmator, 9. deammoniation tower reboiler;
3. one-level feed preheater, 301. one-level feed preheater material inlets, 302. one-level feed preheater material outlets, the deamination tower bottoms import of 303. one-level feed preheaters, the deamination tower bottoms outlet of 304. one-level feed preheaters;
4. secondary raw materials preheater, 401. secondary raw materials preheater material inlets, 402. secondary raw materials preheater material outlets, 403. depickling tower bottoms imports, 404. depickling tower bottoms outlets;
6. condensate cooler, 601. condensate cooler imports, 602. condensate cooler ammoniacal liquor outlets;
7. still liquid water cooler, 701. deamination tower bottoms imports, 702. deamination tower bottoms outlets;
10. ammoniacal liquor surge tank, 1001. ammoniacal liquor dashpot ammoniacal liquor imports, 1002. ammoniacal liquor dashpot ammoniacal liquor outlets, 1003. non-condensable gas entrances, 1004. non-condensable gas outlets;
11. ammonia vessels, 12. lye vats, 13. feedstock pumps, 14. depickling tower reactor liquid pumps, 15. add alkali pump, 16. ammoniacal liquor Loading Pump.
Embodiment
In the present embodiment, the sulfide content of pending waste water is 20000-50000ppm, and ammonia-nitrogen content is 15000-30000ppm,
The technical process of the wastewater preprocessing process that the present embodiment provides as shown in Figure 1, the equipment that described technique needs comprises extracting tower 1, deammoniation tower 2, one-level feed preheater 3, secondary raw materials preheater 4, dephlegmator 5, condensate cooler 6, still liquid water cooler 7, extracting tower reboiler 8, deammoniation tower reboiler 9, ammoniacal liquor surge tank 10, ammonia vessel 11, lye vat 12, feedstock pump 13, depickling tower reactor liquid pump 14, adds alkali pump 15, ammoniacal liquor Loading Pump 16
The operating process of described technique is as follows
1), temperature is that the raw material waste water of 25-30 DEG C is after feedstock pump 13, be divided into cold, heat two bursts of chargings, one-level feed preheater 3 is entered by one-level feed preheater material inlet 301 as one of hot feed, 65-70 DEG C is warming up to after the deamination tower bottoms entered with the deamination tower bottoms import 303 of one-level feed preheater carries out a heat exchange, raw material waste water enters secondary raw materials preheater 4 through secondary raw materials preheater material inlet 401 after being flowed out by one-level feed preheater material outlet 302 after a heat exchange, and carry out secondary heat exchange with the depickling tower bottoms that the depickling tower bottoms import 403 by secondary raw materials preheater enters, 105-110 DEG C is increased to by the raw material wastewater temperature of the outflow of secondary raw materials preheater material outlet 402 after secondary heat exchange, then extracting tower is entered as hot feed by the hot feed mouth 102 of extracting tower, raw material waste water as cold feed directly enters extracting tower by tower top by the cold feed mouth 101 being positioned at extracting tower tower top, and raw material waste water flows from top to bottom in extracting tower, under the stripping effect that depickling tower bottom reboiler provides thermal source to produce, be rich in H
2the sour gas of S composition exports 103 extraction from extracting tower overhead gas and is sent to desulfurization workshop section
2) export 104 depickling tower bottomss out by depickling tower bottoms exporting 404 from the depickling tower bottoms of secondary raw materials preheater 4 after being cooled to after carrying out heat exchange with raw material waste water wherein flow out through secondary raw materials preheater 4, deammoniation tower is entered by deammoniation tower import 201 with self-pressure, deammoniation tower import is equivalent to the 20-30% of the total stage number of deammoniation tower apart from head tray number, meanwhile add by the alkali lye adding storage in lye vat 12 that alkali pump 15 extracts, this alkali lye enters deammoniation tower through adding alkali mouth 202, add alkali mouth and deammoniation tower import is positioned at above same column plate, under the stripping effect that deamination tower bottom reboiler provides thermal source to produce, rich ammonia gas is from overhead extraction, dephlegmator 5 through being positioned at deammoniation tower tower top cools rear section gas becomes liquid phase, as backflow, all the other rich ammonia gas enter condensate cooler 6 through dephlegmator pneumatic outlet 501 by condensate cooler import 601, after circulating water, condensation becomes liquid phase, described liquid phase enters ammoniacal liquor surge tank 10 through ammoniacal liquor dashpot ammoniacal liquor import 1001 after exporting 602 outflows by condensate cooler ammoniacal liquor, then export 1002 by ammoniacal liquor dashpot ammoniacal liquor to flow into as product ammoniacal liquor inflow ammonia vessel 11, the ammoniacal liquor in ammonia vessel can transport through ammoniacal liquor Loading Pump 16 entrucking,
The non-condensable gas in condensate cooler condensation process in rich ammonia gas enters ammoniacal liquor surge tank 10 by the non-condensable gas entrance 1003 of ammoniacal liquor surge tank, and exported together with 1004 non-condensable gases of discharging with the venting port of ammonia vessel 11 by the non-condensable gas of ammoniacal liquor surge tank 10 and enter absorption section
The waste water eventually passing through deammoniation tower process enters one-level feed preheater 3 through deamination tower bottoms outlet 203 by deamination tower bottoms import 303, with raw material waste water after first time heat exchange, after the deamination tower bottoms outlet 304 of one-level feed preheater is flowed out, enter deamination tower reactor liquid cooling but device 7 by deamination tower bottoms import 701, after circulating water is to 30-35 DEG C, enters biochemical workshop section by deamination tower bottoms outlet 702;
The throughput ratio of the hot and cold charging of described extracting tower is 0.1-0.4, preferred 0.1-0.2.
Described deammoniation tower tower bottoms tower exit temperature is 134.5-138 DEG C, and described extracting tower tower bottoms temperature tower exit temperature is 155-160 DEG C, and accordingly, deammoniation tower working pressure is 0.2-0.25Mpa, and extracting tower working pressure controls at below 0.6Mpa.
The pipeline centre being exported to deammoniation tower import 201 at the depickling tower bottoms of secondary raw materials preheater 4 is also provided with depickling tower reactor liquid pump 14.For carrying out pumping charging when self-pressure cannot complete deammoniation tower charging.
In the technique of the present embodiment, described deammoniation tower, extracting tower are stripping tower, are preferably the stripping tower disclosed in first patent CN201120051128.2 of applicant's application.
The column plate of described deammoniation tower, extracting tower adopts film spray no-back mixing column plate, described film spray no-back mixing column plate as applicant apply for described in first patent CN200920095625.5.
Through the waste water of deammoniation tower process, its sulfide content is down to below 50ppm, and ammonia-nitrogen content is down to below 150ppm.
Ppm and mg/L described in this specification sheets, described sulfide content is all with S
2-meter.
Claims (6)
1. the pretreatment technology of a waste water, the equipment that described technique needs comprises extracting tower, deammoniation tower, one-level feed preheater, secondary raw materials preheater, dephlegmator, condensate cooler, still liquid water cooler, extracting tower reboiler, deammoniation tower reboiler, ammoniacal liquor surge tank, ammonia vessel, lye vat, feedstock pump, adds alkali pump, described extracting tower, deammoniation tower are rectifying tower
The operating process of described technique is as follows
1), temperature is that the raw material waste water of 25-30 DEG C is after feedstock pump, be divided into cold, heat two bursts of chargings, one-level feed preheater is entered by one-level feed preheater material inlet as one of hot feed, 65-70 DEG C is warming up to after the deamination tower bottoms entered with the deamination tower bottoms import of one-level feed preheater carries out a heat exchange, raw material waste water enters secondary raw materials preheater through secondary raw materials preheater material inlet after being flowed out by one-level feed preheater material outlet after a heat exchange, and carry out secondary heat exchange with the depickling tower bottoms that the depickling tower bottoms import by secondary raw materials preheater enters, 105-110 DEG C is increased to by the raw material wastewater temperature of the outflow of secondary raw materials preheater material outlet after secondary heat exchange, then extracting tower is entered as hot feed by the hot feed mouth of extracting tower, raw material waste water as cold feed directly enters extracting tower by tower top by the cold feed mouth being positioned at extracting tower tower top, and raw material waste water flows from top to bottom in extracting tower, under the stripping effect that depickling tower bottom reboiler provides thermal source to produce, be rich in H
2the sour gas of S composition is sent to other workshop sections from extracting tower overhead gas outlet extraction
2) the depickling tower bottoms being exported out by depickling tower bottoms is exporting from the depickling tower bottoms of secondary raw materials preheater after being cooled to after carrying out heat exchange with raw material waste water wherein flowing out through secondary raw materials preheater, deammoniation tower is entered by deammoniation tower import with self-pressure, deammoniation tower import is equivalent to the 20-30% of the total stage number of deammoniation tower apart from head tray number, meanwhile add by adding the alkali lye stored in the lye vat of alkali pump extraction, this alkali lye enters deammoniation tower through adding alkali mouth, add alkali mouth and deammoniation tower import is positioned at above same column plate, under the stripping effect that deamination tower bottom reboiler provides thermal source to produce, rich ammonia gas is from overhead extraction, dephlegmator cooling rear section gas through being positioned at deammoniation tower tower top becomes liquid phase, as backflow, all the other rich ammonia gas enter condensate cooler through dephlegmator pneumatic outlet by condensate cooler import, after circulating water, condensation becomes liquid phase, described liquid phase enters ammoniacal liquor surge tank through the import of ammoniacal liquor dashpot ammoniacal liquor after exporting outflow by condensate cooler ammoniacal liquor, is then exported to flow into by ammoniacal liquor dashpot ammoniacal liquor to flow into ammonia vessel as product ammoniacal liquor,
The non-condensable gas in condensate cooler condensation process in rich ammonia gas enters ammoniacal liquor surge tank by the non-condensable gas entrance of ammoniacal liquor surge tank, and is exported by the non-condensable gas of ammoniacal liquor surge tank together with the non-condensable gas of discharging with the venting port of ammonia vessel and enter other workshop sections,
The waste water eventually passing through deammoniation tower process enters one-level feed preheater through the outlet of deamination tower bottoms by the import of deamination tower bottoms, with raw material waste water after first time heat exchange, after the deamination tower bottoms outlet of one-level feed preheater is flowed out, enter deamination tower reactor liquid cooling but device by the import of deamination tower bottoms, after circulating water is to 30-35 DEG C, enters other workshop sections by the outlet of deamination tower bottoms;
The throughput ratio of the hot and cold charging of described extracting tower is 0.1-0.4, and described deammoniation tower tower bottoms tower exit temperature is 134.5-138 DEG C, and described extracting tower tower bottoms temperature tower exit temperature is 155-160 DEG C.
2. technique as claimed in claim 1, is characterized in that the throughput ratio of the hot and cold charging of extracting tower is 0.1-0.2.
3. technique as claimed in claim 1, is characterized in that described deammoniation tower, extracting tower all adopt the plate distillation column of application film spray no-back mixing column plate.
4. technique as claimed in claim 1, is characterized in that described deammoniation tower, extracting tower all adopts stripping tower.
5. technique as claimed in claim 3, is characterized in that described deammoniation tower, extracting tower all adopt the panel type steam stripper of application film spray no-back mixing column plate.
6. the technique as described in as arbitrary in Claims 1 to 5, it is characterized in that described high-sulfur compound, the sulfide content of high ammonia-nitrogen wastewater is 20000-50000ppm, ammonia-nitrogen content is 15000-30000ppm, and the waste water sulfide amount eventually passing through deammoniation tower process is down to below 50ppm (with H
2s counts), ammonia-nitrogen content is down to below 150ppm.
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| CN201510162109.XA CN104787954A (en) | 2015-04-08 | 2015-04-08 | Wastewater pretreatment technology |
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| CN105884106A (en) * | 2016-04-22 | 2016-08-24 | 唐山旭阳化工有限公司 | Benzene hydrogenation wastewater desulfurization and deamination treatment method aiming at improving deamination and treatment device applying same |
| CN106315726A (en) * | 2016-10-12 | 2017-01-11 | 江苏金茂源生物化工有限责任公司 | Biogas slurry decarbonization and deamination combined system |
| CN106554115A (en) * | 2016-12-08 | 2017-04-05 | 西安润格环保科技有限公司 | A kind of coal chemical industrial waste water is reduced pressure depickling deamination method and system step by step |
| CN106629937A (en) * | 2015-11-02 | 2017-05-10 | 中国石油化工股份有限公司 | Waste water processing technology and system |
| CN107324284A (en) * | 2017-07-07 | 2017-11-07 | 天津市职业大学 | A kind of system of recycling treatment iron-contained industrial waste hydrochloric acid |
| CN107413194A (en) * | 2016-12-29 | 2017-12-01 | 天津市创举科技股份有限公司 | Preparation method and equipment of concentrated ammonia water for desulfurization and denitrification |
| CN109111006A (en) * | 2018-09-21 | 2019-01-01 | 河南龙成煤高效技术应用有限公司 | A kind of method and equipment recycling ammonia from pyrolysis of coal waste water |
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| CN106629937B (en) * | 2015-11-02 | 2020-05-19 | 中国石油化工股份有限公司 | Wastewater treatment process and system |
| CN105884106A (en) * | 2016-04-22 | 2016-08-24 | 唐山旭阳化工有限公司 | Benzene hydrogenation wastewater desulfurization and deamination treatment method aiming at improving deamination and treatment device applying same |
| CN106315726A (en) * | 2016-10-12 | 2017-01-11 | 江苏金茂源生物化工有限责任公司 | Biogas slurry decarbonization and deamination combined system |
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| CN107413194A (en) * | 2016-12-29 | 2017-12-01 | 天津市创举科技股份有限公司 | Preparation method and equipment of concentrated ammonia water for desulfurization and denitrification |
| CN107324284A (en) * | 2017-07-07 | 2017-11-07 | 天津市职业大学 | A kind of system of recycling treatment iron-contained industrial waste hydrochloric acid |
| CN109111006A (en) * | 2018-09-21 | 2019-01-01 | 河南龙成煤高效技术应用有限公司 | A kind of method and equipment recycling ammonia from pyrolysis of coal waste water |
| CN109111006B (en) * | 2018-09-21 | 2022-01-07 | 河南龙成煤高效技术应用有限公司 | Method and equipment for recovering ammonia gas from coal pyrolysis wastewater |
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Address after: 300130 the Binhai New Area of Tianjin Huayuan Industrial Zone (outer ring) Hai Tai innovation six road No. 2 15-1 Applicant after: Tianjin pioneering Polytron Technologies Inc Address before: 300130 East Hospital, Hebei University of Technology, 8 glorious road, Hongqiao, Tianjin Applicant before: Tianjin Chuangju Science and Technology Co., Ltd. |
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