CN104986816B - Process and apparatus for carrying out wastewater desorption and falling film evaporation on coking sewage - Google Patents
Process and apparatus for carrying out wastewater desorption and falling film evaporation on coking sewage Download PDFInfo
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- CN104986816B CN104986816B CN201510084437.2A CN201510084437A CN104986816B CN 104986816 B CN104986816 B CN 104986816B CN 201510084437 A CN201510084437 A CN 201510084437A CN 104986816 B CN104986816 B CN 104986816B
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- waste water
- falling film
- desorber
- film evaporator
- steam
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- 239000002351 wastewater Substances 0.000 title claims abstract description 144
- 239000011552 falling film Substances 0.000 title claims abstract description 63
- 238000003795 desorption Methods 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000010865 sewage Substances 0.000 title claims abstract description 31
- 238000001704 evaporation Methods 0.000 title claims description 19
- 230000008020 evaporation Effects 0.000 title claims description 19
- 238000004939 coking Methods 0.000 title abstract description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 90
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 43
- 239000007788 liquid Substances 0.000 claims abstract description 41
- 238000010438 heat treatment Methods 0.000 claims abstract description 21
- 239000013589 supplement Substances 0.000 claims abstract 2
- 238000004064 recycling Methods 0.000 claims description 27
- 239000002994 raw material Substances 0.000 claims description 26
- 238000000926 separation method Methods 0.000 claims description 21
- 238000005516 engineering process Methods 0.000 claims description 12
- 239000010408 film Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 7
- 239000000571 coke Substances 0.000 claims description 5
- 239000003034 coal gas Substances 0.000 claims description 4
- 238000004891 communication Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 27
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000002918 waste heat Substances 0.000 abstract description 2
- 238000013021 overheating Methods 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 239000006200 vaporizer Substances 0.000 description 6
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000284 extract Substances 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Physical Water Treatments (AREA)
Abstract
The present invention relates to a coking sewage desorption processes, which comprises that 1) coking sewage enters the top portion of a desorption tower, is subjected to steam stripping desorption, and then is discharged from the top portion of the tower; 2) the desorption gas enters a falling film evaporator, and is subjected to heat exchange with high-temperature wastewater to form ammonia vapor with an ammonia concentration of 10-20% and a condensed liquid; 3) the circulating wastewater introduced into the falling film evaporator from the desorption tower is evaporated to produce secondary steam; and 4) the low-temperature secondary steam is compressed into high-temperature and high-pressure overheating steam with a pressure of 0.14-0.6 MPa (A) and a temperature of 110-220 DEG C through a compressor, and is conveyed into the desorption tower as the supplement steam for the heating steam. The apparatus for achieving the process comprises the desorption tower, the falling film evaporator and the compressor. Compared with the process and the apparatus in the prior art, the process and the apparatus of the present invention have the following beneficial effects that the waste heat of the desorption gas on the top portion of the desorption tower can be recovered and utilized, the low-temperature heat source is converted into the high-temperature heat source through the compressor so as to return to the desorption tower and be reused, the consumption of the new steam is reduced by more than or equal to 60-75%, and characteristics of reasonable and compact process, simple operation, less equipment configuration and low investment cost are provided.
Description
Technical field
The present invention relates to coked waste water processing technology field, particularly relate to a kind of coked waste water desorbing waste water falling film evaporation technology and
Device.
Background technology
The coked waste water that coking production process produces mainly includes coking coal surface water, coking water of constitution and pollution discharge water, burnt
Change sewage impurities complicated component, mainly contain H2S、NH3, HCN, the component such as phenols and polycyclic aromatic hydrocarbon.Coking is dirty
Water processes and mainly comprises the processes of solvent method dephenolize, desorption method removing H2S、NH3, HCN, biological degradation method reduce efflux wastewater
COD, wherein desorption method is one of important procedure of sewage disposal, its thermal energy consumption (steam consumption, gas consumption etc.)
The cost processing overall process with coked waste water is closely related.
At present, coked waste water desorption technique generally uses desorption method to remove H therein2S、NH3, the component such as HCN, main work
Skill process is: after at the bottom of coked waste water and desorber, wastewater heat exchange heats up, and sends into desorber top, and in desorber with rising
Steam counter-flow contacts and is heated, strips, and desorbing tower top produces containing NH3、H2S、HCN、H2The stripping gas of the components such as O
Body, enters ammonia dephlegmator；In ammonia dephlegmator utilize cooling water by desorption gas cool down, condensing, the ammonia vapour of condensing generation send
To coke oven gas system, dephlegmator condensed liquid backflow desorbing tower top, the hot waste water produced at the bottom of desorber send biochemistry after cooling
Treatment process.
Increase the quantity of steam at the bottom of desorber and can be effectively reduced impurity content in waste water, but also can increase the life of desorption step accordingly
Producing cost, therefore the improvement to coked waste water desorption technique is devoted to while improving desorption efficiency to reduce disappearing of heat energy always
Consumption.
The Chinese patent of Application No. 201210275298.8 (filing date on August 3rd, 2012) discloses " a kind of surplus
Remaining ammonia heat pump distillation system ", " steam (vapor) outlet at original ammonia still top is simultaneously connected to heat pump and point contracting by three-way valve
Steam in device, heat pump and dephlegmator is pooled to cooler, and the ammonia in cooler sequentially passes through finished product ammonia vessel backward
With remove desulfurizer after reflux pump ".Described in this patent, remained ammonia heat pump distillation system is to utilize tower top by absorption heat pump
Ammonia vapour heat is for heating at the bottom of tower.Working medium in absorption heat pump is in ammonia vapour heat exchanger and ammonia vapour heat exchange, working medium absorbing ammonia vapour heat
Amount is vaporized into steam, and steam delivers to cooler through compressor pressurization again；Ammonia vapour is condensed into ammonia, and partial ammonia water refluxes, sends outside.
Waste water at the bottom of tower send the steam of cooler cooling compression, and waste water absorbs heat and returns at the bottom of ammonia still.Absorption heat pump heat in this system
Amount transfer is to be realized by twice heat exchange (ammonia vapour working medium, working medium waste water), there is system operation complexity, equipment throwing
The problem that money is high, heat utilization ratio is low.These problems greatly hinder the popularization and application at coking industry of this system.
Summary of the invention
The invention provides a kind of coked waste water desorbing waste water falling film evaporation technology, the waste heat of desorbing tower top desorption gas can be returned
Receive and utilize, and by compressor, low-temperature heat source is converted into high temperature heat source and returns desorber and use, minimizing initial steam consumption 60～
More than 75%, and flow process is the compactest, simple to operate, equipment configures less, input cost is low；Invention also provides use
In the device realizing this technique.
In order to achieve the above object, the present invention realizes by the following technical solutions:
A kind of coked waste water desorbing waste water falling film evaporation technology, comprises the steps:
1) coked waste water after heat exchange enters desorber top, adds vapours and enters at the bottom of desorber, the NH in coked waste water3、
H2The components such as S, HCN desorption gas after steam stripping desorbing is discharged by tower top；
2) desorption gas gone out from desorber top row enters the heating chamber of falling film evaporator, the part hot waste water at the bottom of desorber
Forming ammonia density after entering the separation chamber of falling film evaporator, desorption gas and wastewater heat exchange is 10～the ammonia vapour of 20% and condensed liquid；
Wherein ammonia vapour send coke oven gas system, and condensed liquid flows in raw material sump and collects with coked waste water, then by raw material sewage pump
Send sewage/wastewater heat exchange device, after the hot waste water heat exchange extracted out at the bottom of desorber, enter desorber top with by waste water pump；Change
Waste water after heat drop temperature send biochemical operation to process further；
3) introduce the recycling waste water recycling waste water bottom falling film evaporator from desorber and be pumped to the liquid at falling film evaporator top
Body distribution apparatus enters heating pipe after forming uniform liquid film, and part evaporation produces low temperature indirect steam in pipe；Low temperature secondary
Steam and recycling waste water flow into separation chamber in the lump, and the low temperature indirect steam after gas-liquid separation sends into compressor；
4) low temperature indirect steam boil down to pressure is 0.14～0.6MPa (A) by compressor, temperature 110～the high temperature of 220 DEG C
High pressure superheated steam also sends into desorber as the supplementary steam adding vapours.
The desorption gas temperature that desorber top row goes out is 95～135 DEG C, and condensing rear ammonia stripping temperature is 90～115 DEG C, desorber
End hot waste water temperature is 98～155 DEG C, falling film evaporator add the low temperature indirect steam temperature produced in heat pipe be 75～
110℃。
For realizing the device of a kind of coked waste water desorbing waste water falling film evaporation technology, including by the desorber of pipeline communication,
Falling film evaporator and compressor, the desorption gas outlet of described desorber tower top connects the gas of falling film evaporator heating chamber and enters
Mouthful, the steam (vapor) outlet of falling film evaporator connects the steam inlet of compressor, and the steam (vapor) outlet of compressor connects to be mended bottom desorber
Fill steam inlet；The ammonia vapor outlet of falling film evaporator additionally connects coal gas system, and the condensed liquid outlet of falling film evaporator connects former
Material sump；The recycling waste water entrance of falling film evaporator separator connects the hot waste water outlet of desorber bottom, falling film evaporator
Recycling waste water pump is set in bottom separation chamber and overhead-liquid distribution apparatus connecting pipe.
Described raw material sump is additionally provided with coked waste water entrance, and the coked waste water of raw material sump exports by raw material sewage
Pump, sewage/wastewater heat exchange device connection desorber top coked waste water entrance, sewage/wastewater heat exchange device is additionally by waste water pump even
General solution inhales the outlet of tower bottom hot waste water.
Compared with prior art, the invention has the beneficial effects as follows:
1) heat recovery to desorbing tower top desorption gas, produces low temperature indirect steam by heat cycles waste water, adopts
With compressor to low temperature indirect steam compressed action so that it is become high-temperature high-pressure overheat steam and make as thermal source return desorber
With, reduce initial steam consumption 60～more than 75%；
2) using falling film evaporator evaporation, evaporability is strong, and heat utilization efficiency is high, can improve desorption efficiency, reduces ammonia still process and gives up
Water impurity content；
3) falling film evaporator uses the mode being circulated heat exchange from desorber extraction hot waste water, it is not necessary to draw outward circulating cooling
Water, energy-saving and cost-reducing；
4) desorber tower top is without backflow, can improve sewage desorption efficiency；
5) technological process is the compactest, simple to operate, and equipment configures less, input cost is low.
Accompanying drawing explanation
Fig. 1 is the general flow chart of technique of the present invention.
In figure: 1. desorber 2. falling film evaporator 3. sewage/wastewater heat exchange device 4. compressor 5. raw material sump 6.
Waste water pump 7. recycling waste water pump 8. raw material sewage pump
Detailed description of the invention
Below in conjunction with the accompanying drawings the detailed description of the invention of the present invention is described further:
See Fig. 1, be the general flow chart of technique of the present invention, a kind of coked waste water desorbing waste water falling film evaporation of the present invention
Technique, comprises the steps:
1) coked waste water after heat exchange enters desorber 1 top, adds vapours and enters at the bottom of desorber, the NH in coked waste water3、
H2The components such as S, HCN desorption gas after steam stripping desorbing is discharged by tower top；
2) desorption gas gone out from desorber top row enters the heating chamber of falling film evaporator 2, and the part high temperature at the bottom of desorber gives up
Water forms ammonia density after entering the separation chamber of falling film evaporator 2, desorption gas and wastewater heat exchange be 10～the ammonia vapour of 20% and coagulating
Contracting liquid；Wherein ammonia vapour send coke oven gas system, and condensed liquid flows in raw material sump 5 and collects with coked waste water, then by former
Material sewage pump 8 send sewage/wastewater heat exchange device 3, laggard from the hot waste water heat exchange extracted out at the bottom of desorber with by waste water pump 6
Enter desorbing tower top；Waste water after heat exchange cooling send biochemical operation to process further；
3) falling film evaporator 2 delivered to by the recycling waste water recycling waste water pump 7 introduced bottom falling film evaporator 2 from desorber 1
The liquid distribution device at top enters heating pipe after forming uniform liquid film, and part evaporation produces low temperature indirect steam in pipe；
Low temperature indirect steam and recycling waste water flow into separation chamber in the lump, and the low temperature indirect steam after gas-liquid separation sends into compressor 4；
4) low temperature indirect steam boil down to pressure is 0.14～0.6MPa (A) by compressor 4, temperature 110～the height of 220 DEG C
Temperature high pressure superheated steam also sends into desorber 1 as the supplementary steam adding vapours.
The desorption gas temperature that desorber top row goes out is 95～135 DEG C, and condensing rear ammonia stripping temperature is 90～115 DEG C, desorber
End hot waste water temperature is 98～155 DEG C, falling film evaporator 2 add the low temperature indirect steam temperature produced in heat pipe be 75～
110℃。
For realizing the device of a kind of coked waste water desorbing waste water falling film evaporation technology, including by the desorber 1 of pipeline communication,
Falling film evaporator 2 and compressor 4, the desorption gas outlet of described desorber 1 tower top connects falling film evaporator 2 heating chamber
Gas access, the steam (vapor) outlet of falling film evaporator 2 connects the steam inlet of compressor 4, and the steam (vapor) outlet of compressor 4 connects
Steam inlet is supplemented bottom desorber 1；The ammonia vapor outlet of falling film evaporator 2 additionally connects coal gas system, falling film evaporator 2
Condensed liquid outlet connect tar stock sump 5；The recycling waste water entrance of falling film evaporator 2 separator connects desorber 1
Bottom hot waste water outlet, sets recycling waste water on separation chamber and overhead-liquid distribution apparatus connecting pipe bottom falling film evaporator 2
Pump 7.
Described raw material sump 5 is additionally provided with coked waste water entrance, and the coked waste water outlet of raw material sump 5 is dirty by raw material
Water pump 8, sewage/wastewater heat exchange device 3 connects desorber 1 top coked waste water entrance, and sewage/wastewater heat exchange device 3 additionally leads to
Cross waste water pump 6 and connect hot waste water outlet bottom desorber 1.
Following example are implemented under premised on technical solution of the present invention, give detailed embodiment and concrete
Operating process, but protection scope of the present invention is not limited to following embodiment.In following embodiment, method therefor is as without saying especially
Bright it is conventional method.
[embodiment 1]
Coked waste water enters in raw material sump 5, extracts out with raw material sewage pump 8 and send sewage/wastewater heat exchange device 3 to give up with high temperature
After water heat exchange is warming up to 97 DEG C, send into desorber 1 top, in Ta Nei and upflowing vapor counter current contacting, by heating, vapour
The effect that carries is with desorbing NH contained therein3、H2The components such as S, HCN.
Gained hot waste water temperature 105 DEG C after desorbing, major part is dirty with coking through sewage/wastewater heat exchange device 3 with waste water pump 6
Sending biochemical operation to process further after water heat exchange cooling, small part hot waste water enters the separation chamber of falling film evaporator 2.Falling liquid film
Recycling waste water recycling waste water pump 7 bottom vaporizer 2 is delivered to the liquid distribution device at vaporizer 2 top and is formed uniform liquid film
Entrance adds heat pipe, and part evaporation produces 0.085MPa (A), the low temperature indirect steam of 95 DEG C in pipe.
Low temperature indirect steam and recycling waste water flow into the separation chamber of falling film evaporator 2 in the lump, and after this gas-liquid separation, steam enters
Enter compressor 4, by compressor 4 to its compressed action so that it is become 0.15MPa (A), the superheated steam of 125 DEG C.Pressure
The superheated steam of contracting machine 4 output enters desorber 1 and heats upflowing vapor needed for the generation desorbing of tower reactor waste water.
The 0.12MPa (A) that desorber 1 top produces, the desorption gas of 103 DEG C enter the heating chamber of falling film evaporator 2, heating
It is cooled to 99 DEG C while recycling waste water, forms condensed liquid and the ammonia vapour of ammonia density 15%.Ammonia vapour send coke oven gas system,
Condensed liquid flows in raw material sump 5.
[embodiment 2]
Coked waste water enters in raw material sump 5, extracts out with raw material sewage pump 8 and send sewage/wastewater heat exchange device 3 to give up with high temperature
After water heat exchange is warming up to 98 DEG C, send into desorber 1 top, in Ta Nei and upflowing vapor counter current contacting, by heating, vapour
The effect that carries is with desorbing NH contained therein3、H2The components such as S, HCN.
Gained hot waste water temperature 106 DEG C after desorbing, major part is dirty with coking through sewage/wastewater heat exchange device 3 with waste water pump 6
Sending biochemical operation to process further after water heat exchange cooling, small part hot waste water enters the separation chamber of falling film evaporator 2.Falling liquid film
Recycling waste water recycling waste water pump 7 bottom vaporizer 2 is delivered to the liquid distribution device at vaporizer 2 top and is formed uniform liquid film
Entrance adds heat pipe, and part evaporation produces 0.051MPa (A), the low temperature indirect steam of 82 DEG C in pipe.
Low temperature indirect steam and recycling waste water flow into the separation chamber of falling film evaporator 2 in the lump, and after this gas-liquid separation, steam enters
Enter compressor 4, by compressor 4 to its compressed action so that it is become 0.157MPa (A), the superheated steam of 135 DEG C.Pressure
The superheated steam of contracting machine output enters desorber 1 and heats upflowing vapor needed for the generation desorbing of tower reactor waste water.
The 0.125MPa (A) that desorber 1 top produces, the desorption gas of 103.5 DEG C enter the heating chamber of falling film evaporator 2,
It is cooled to 98 DEG C while heat cycles waste water, forms condensed liquid and the ammonia vapour of ammonia density 15.2%.Ammonia vapour send coke-oven coal
Gas system, condensed liquid flows in raw material sump 5.
[embodiment 3]
Coked waste water enters in raw material sump 5, extracts out with raw material sewage pump 8 and send sewage/wastewater heat exchange device 3 to give up with high temperature
After water heat exchange is warming up to 106 DEG C, send into desorber 1 top, in Ta Nei and upflowing vapor counter current contacting, by heating, vapour
The effect that carries is with desorbing NH contained therein3、H2The components such as S, HCN.
Gained hot waste water temperature 114 DEG C after desorbing, major part is dirty with coking through sewage/wastewater heat exchange device 3 with waste water pump 6
Sending biochemical operation to process further after water heat exchange cooling, small part hot waste water enters the separation chamber of falling film evaporator 2.Falling liquid film
Recycling waste water recycling waste water pump 7 bottom vaporizer 2 is delivered to the liquid distribution device at vaporizer 2 top and is formed uniform liquid film
Entrance adds heat pipe, and part evaporation produces 0.096MPa (A), the low temperature indirect steam of 98 DEG C in pipe.
Low temperature indirect steam and recycling waste water flow into the separation chamber of falling film evaporator 2 in the lump, and after this gas-liquid separation, steam enters
Enter compressor 4, by compressor 4 to its compressed action so that it is become 0.19MPa (A), the superheated steam of 142 DEG C.Pressure
The superheated steam of contracting machine 4 output enters desorber 1 and heats upflowing vapor needed for the generation desorbing of tower reactor waste water.
The 0.15MPa (A) that desorber 1 top produces, the desorption gas of 108 DEG C enter the heating chamber of falling film evaporator 2, heating
It is cooled to 105 DEG C while recycling waste water, forms condensed liquid and the ammonia vapour of ammonia density 18%.Ammonia vapour send coke-stove gas system
System, condensed liquid flows in raw material sump 5.
Claims (4)
1. a coked waste water desorbing waste water falling film evaporation technology, it is characterised in that comprise the steps:
1) coked waste water after heat exchange enters desorber top, and heating steam enters at the bottom of desorber, the NH in coked waste water3、H2S, HCN desorption gas after steam stripping desorbing is discharged by tower top；
2) desorption gas gone out from desorber top row enters the heating chamber of falling film evaporator, and the part hot waste water at the bottom of desorber enters the separation chamber of falling film evaporator, and forming ammonia density after desorption gas and wastewater heat exchange is 10～the ammonia of 20% and condensed liquid；Wherein ammonia send coke oven gas system, and condensed liquid flows in raw material sump and collects with coked waste water, is then pumped sewage/wastewater heat exchange device by raw material sewage, enters desorber top with by waste water pump after the hot waste water heat exchange extracted out at the bottom of desorber；Waste water after heat exchange cooling send biochemical operation to process further；
3) introduce the recycling waste water recycling waste water bottom falling film evaporator from desorber to be pumped to enter heating pipe, and part evaporation generation low temperature secondary steam in pipe after the liquid distribution device at falling film evaporator top forms uniform liquid film；Low temperature secondary steam and recycling waste water flow into separation chamber in the lump, and the low temperature secondary steam after gas-liquid separation sends into compressor；
4) low temperature secondary steam boil down to pressure is 0.14～0.6MPaA by compressor, and temperature 110～the High Temperature High Pressure superheated vapor of 220 DEG C also send into the desorber supplementary steam as heating steam.
A kind of coked waste water desorbing waste water falling film evaporation technology the most according to claim 1, it is characterized in that, the desorption gas temperature that desorber top row goes out is 95～135 DEG C, condensing rear ammonia temperature is 90～115 DEG C, hot waste water temperature at the bottom of desorber is 98～155 DEG C, and the low temperature secondary steam temperature that falling film evaporator produces in adding heat pipe is 75～110 DEG C.
A kind of coked waste water desorbing waste water falling film evaporation technology the most according to claim 1, it is characterized in that, the device used includes by the desorber of pipeline communication, falling film evaporator and compressor, the desorption gas outlet of described desorber tower top connects the gas access of falling film evaporator heating chamber, the vapor outlet port of falling film evaporator connects the vapour inlet of compressor, and the vapor outlet port of compressor connects supplements vapour inlet bottom desorber；The ammonia outlet of falling film evaporator additionally connects coal gas system, and the condensed liquid outlet of falling film evaporator connects raw material sump；The recycling waste water entrance of falling film evaporator separator connects the hot waste water outlet of desorber bottom, sets recycling waste water pump bottom falling film evaporator on separation chamber and overhead-liquid distribution apparatus connecting pipe.
A kind of coked waste water desorbing waste water falling film evaporation technology the most according to claim 3, it is characterized in that, described raw material sump is additionally provided with coked waste water entrance, the coked waste water outlet of raw material sump is by raw material sewage pump, sewage/wastewater heat exchange device connection desorber top coked waste water entrance, and sewage/wastewater heat exchange device is additionally by hot waste water outlet bottom waste water pump connection desorber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510084437.2A CN104986816B (en) | 2015-02-16 | 2015-02-16 | Process and apparatus for carrying out wastewater desorption and falling film evaporation on coking sewage |
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| CN201510084437.2A CN104986816B (en) | 2015-02-16 | 2015-02-16 | Process and apparatus for carrying out wastewater desorption and falling film evaporation on coking sewage |
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| CN104986816B true CN104986816B (en) | 2017-01-11 |
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| CN105906123B (en) * | 2016-05-26 | 2018-06-19 | 苏州派宁环保科技有限公司 | The system and method for processing wastewater from chemical industry based on stripping and MVR group technologies |
| CN108069479B (en) * | 2016-11-11 | 2020-01-10 | 中国石油化工股份有限公司抚顺石油化工研究院 | Wastewater treatment method and system |
| CN108069482B (en) * | 2016-11-11 | 2020-01-10 | 中国石油化工股份有限公司抚顺石油化工研究院 | Wastewater treatment process and system |
| CN112973387A (en) * | 2021-04-08 | 2021-06-18 | 四川金象赛瑞化工股份有限公司 | Combined treatment method and system for waste water and waste gas |
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| JP2005098551A (en) * | 2003-09-22 | 2005-04-14 | Minoru Morita | Method and facility for recovering energy generated in sewage treatment plant |
| CN102241418A (en) * | 2011-05-20 | 2011-11-16 | 新煤化工技术（上海）有限公司 | Negative pressure distillation equipment and method for residual ammonia water |
| CN102671510B (en) * | 2011-11-29 | 2015-08-12 | 中国石油化工股份有限公司 | The recovery process of flue gas CO2 |
| CN203411359U (en) * | 2013-07-31 | 2014-01-29 | 张卫东 | Device for processing residual ammonia water of coke oven with negative pressure flash evaporation method |
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Effective date of registration: 20190528 Address after: 116000 High-tech Industrial Park, Dalian City, Liaoning Province, 126 Gaoneng Street, Unit 3, Floor 2 Patentee after: DALIAN HAOTONG ENVIRONMENTAL PROTECTION ENGINEERING TECHNOLOGY Co.,Ltd. Address before: 114001 Shengli South Road, Tiedong District, Anshan City, Liaoning Province Patentee before: Wu Dachuan |
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