CN104986816A - 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
- Publication number
- CN104986816A CN104986816A CN201510084437.2A CN201510084437A CN104986816A CN 104986816 A CN104986816 A CN 104986816A CN 201510084437 A CN201510084437 A CN 201510084437A CN 104986816 A CN104986816 A CN 104986816A
- Authority
- CN
- China
- Prior art keywords
- waste water
- desorption
- falling
- steam
- film evaporator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 154
- 238000003795 desorption Methods 0.000 title claims abstract description 103
- 239000011552 falling film Substances 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000010865 sewage Substances 0.000 title claims abstract description 23
- 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 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 82
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 38
- 238000010438 heat treatment Methods 0.000 claims abstract description 33
- 239000002994 raw material Substances 0.000 claims description 25
- 238000004064 recycling Methods 0.000 claims description 25
- 238000005516 engineering process Methods 0.000 claims description 12
- 239000000571 coke Substances 0.000 claims description 7
- 239000010408 film Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 4
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 239000003034 coal gas Substances 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 2
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 abstract 2
- 238000013021 overheating Methods 0.000 abstract 1
- 239000013589 supplement Substances 0.000 abstract 1
- 239000002918 waste heat Substances 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 238000010521 absorption reaction Methods 0.000 description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 239000006200 vaporizer Substances 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- 238000004821 distillation Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011084 recovery 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
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
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 desorb waste water falling film evaporation technology and device.
Background technology
The coked waste water that coking production process produces mainly comprises coking coal surface water, coking constitution water and pollution discharge water, coked waste water impurities complicated component, mainly containing H
2s, NH
3, HCN, the component such as phenols and polynuclear aromatics.Coked waste water process main process is: solvent method dephenolize, desorption method removes H
2s, NH
3, HCN, biological degradation method reduces the COD of efflux wastewater, and wherein desorption method is one of important procedure of sewage disposal, and its heat energy consumption (steam consumption, gas consumption etc.) is closely related with the cost of coked waste water process whole process.
At present, coked waste water desorption technique adopts desorption method to remove H wherein usually
2s, NH
3, the component such as HCN, main processes is: after wastewater heat exchange heats up at the bottom of coked waste water and desorption tower, send into desorption tower top, and in desorption tower with upflowing vapor counter current contact and heat, stripping, desorb tower top produces and contains NH
3, H
2s, HCN, H
2the desorption gas of the components such as O, enters ammonia dephlegmator; In ammonia dephlegmator, utilize water coolant to be cooled by desorption gas, condensing, the ammonia vapour of condensing generation delivers to coke oven gas system, and dephlegmator condensed liquid backflow desorb tower top, the hot wastewater produced at the bottom of desorption tower send biochemical treatment operation after cooling.
Increase quantity of steam at the bottom of desorption tower and can effectively reduce foreign matter content in waste water, but also can the production cost of corresponding increase desorption step, therefore the consumption reducing heat energy while improving desorption efficiency is devoted to always to the improvement of coked waste water desorption technique.
Application number is that the Chinese patent of 201210275298.8 (applying date is on August 3rd, 2012) discloses " a kind of remained ammonia heat pump distillation system ", " be connected to heat pump and dephlegmator at the vapour outlet at original ammonia still top by T-valve; the steam in heat pump and dephlegmator is pooled to water cooler, and the ammoniacal liquor in water cooler removes desulfurizer backward successively after finished product ammonia vessel and reflux pump " simultaneously.Remained ammonia heat pump distillation system described in this patent utilizes tower top ammonia vapour heat for heating at the bottom of tower by absorption heat pump.Working medium in absorption heat pump is in ammonia vapour interchanger and the heat exchange of ammonia vapour, and working medium absorbing ammonia vapour heat is vaporized into steam, and steam delivers to water cooler through compressor pressurization again; Ammonia vapour is condensed into ammoniacal liquor, and partial ammonia water refluxes, sends outside.Waste water at the bottom of tower send the steam of water cooler cooled compressed, and waste water absorbs heat and returns at the bottom of ammonia still.In this system, the transfer of absorption heat pump heat is realized by twice heat exchange (ammonia vapour-working medium, working medium-waste water), there is system operation complexity, facility investment is high, heat utilization ratio is low problem.These problems greatly hinder this system applying at coking industry.
Summary of the invention
The invention provides a kind of coked waste water desorb waste water falling film evaporation technology, can by the heat recovery of desorb tower top desorption gas, and low-temperature heat source is converted into high temperature heat source by compressor and returns desorption tower and use, reduce live steam consumption more than 60 ~ 75%, and flow process is rationally compact, simple to operate, Equipments Setting is few, input cost is low; Invention also provides the device for 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 desorb waste water falling film evaporation technology, comprises the steps:
1) coked waste water after heat exchange enters desorption tower top, and heating steam enters at the bottom of desorption tower, the NH in coked waste water
3, H
2the components such as S, HCN desorption gas after steam stripped desorb is discharged by tower top;
2) desorption gas of discharging from desorb tower top enters the heating chamber of falling-film evaporator, and the part hot wastewater at the bottom of desorption tower enters the separate chamber of falling-film evaporator, forms ammonia vapour and the condensed liquid that ammonia density is 10 ~ 20% after desorption gas and wastewater heat exchange; 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 pumping sewage/wastewater heat exchange device, enters desorption tower top with after the hot wastewater heat exchange of being extracted out at the bottom of desorption tower by waste water pump; Waste water after heat exchange cooling send biochemical operation to process further;
3) enter heating tube be pumped to the liquid distribution device formation uniform liquid film at falling-film evaporator top from the desorption tower recycling waste water recycling waste water introduced bottom falling-film evaporator after, and part evaporation produces low temperature secondary steam in pipe; Low temperature secondary steam and recycling waste water flow into separate 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 ~ 0.6MPa (A) by compressor, and the high-temperature high-pressure overheat steam that temperature is 110 ~ 220 DEG C also sends into the supplementary steam of desorption tower as heating steam.
The desorption gas temperature that desorb tower top is discharged is 95 ~ 135 DEG C, and condensing rear ammonia stripping temperature is 90 ~ 115 DEG C, and hot wastewater temperature at the bottom of desorption tower is 98 ~ 155 DEG C, and the low temperature secondary steam temperature produced in falling-film evaporator heating tube is 75 ~ 110 DEG C.
For realizing a kind of device of coked waste water desorb waste water falling film evaporation technology, comprise by the desorption tower of pipeline communication, falling-film evaporator and compressor, the desorption gas outlet of described desorption tower tower top connects the gas inlet of falling-film evaporator heating chamber, the vapour outlet of falling-film evaporator connects the steam-in of compressor, and the vapour outlet of compressor connects supplementary steam-in bottom desorption tower; The ammonia vapor outlet of falling-film evaporator connects coal gas system in addition, 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 wastewater outlet of desorption tower bottom, bottom falling-film evaporator, separate chamber and overhead-liquid distribution apparatus connecting pipe establishes recycling waste water pump.
Described raw material sump is provided with coked waste water entrance in addition, the coked waste water outlet of raw material sump is communicated with desorption tower top coked waste water entrance by raw material sump pump, sewage/wastewater heat exchange device, and sewage/wastewater heat exchange device is communicated with hot wastewater outlet bottom desorption tower additionally by waste water pump.
Compared with prior art, the invention has the beneficial effects as follows:
1) to the heat recovery of desorb tower top desorption gas, low temperature secondary steam is produced by heating cycle waste water, adopt compressor to low temperature secondary steam compressed action, become high-temperature high-pressure overheat steam and return desorption tower as thermal source and use, reduce live steam consumption more than 60 ~ 75%;
2) adopt falling-film evaporator evaporation, steam capability is strong, and heat utilization efficiency is high, can improve desorption efficiency, reduces distilled ammonia wastewater foreign matter content;
3) falling-film evaporator adopts and draws from desorption tower the mode that hot wastewater carries out cycle heat exchange, without the need to drawing recirculated cooling water outward, energy-saving and cost-reducing;
4) desorption tower tower top is without backflow, can improve sewage desorption efficiency;
5) technical process is rationally compact, simple to operate, and Equipments Setting is few, input cost is low.
Accompanying drawing explanation
Fig. 1 is the general flow chart of technique of the present invention.
In figure: 1. desorption tower 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 sump pump
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described further:
Seeing Fig. 1, is the general flow chart of technique of the present invention, and a kind of coked waste water desorb waste water falling film evaporation technology of the present invention, comprises the steps:
1) coked waste water after heat exchange enters desorption tower 1 top, and heating steam enters at the bottom of desorption tower, the NH in coked waste water
3, H
2the components such as S, HCN desorption gas after steam stripped desorb is discharged by tower top;
2) desorption gas of discharging from desorb tower top enters the heating chamber of falling-film evaporator 2, and the part hot wastewater at the bottom of desorption tower enters the separate chamber of falling-film evaporator 2, forms ammonia vapour and the condensed liquid that ammonia density is 10 ~ 20% after desorption gas and wastewater heat exchange; Wherein ammonia vapour send coke oven gas system, and condensed liquid flows in raw material sump 5 and collects with coked waste water, then send sewage/wastewater heat exchange device 3 by raw material sump pump 8, enters desorption tower top with after the hot wastewater heat exchange of being extracted out at the bottom of desorption tower by waste water pump 6; Waste water after heat exchange cooling send biochemical operation to process further;
3) enter heating tube deliver to the liquid distribution device formation uniform liquid film at falling-film evaporator 2 top from the desorption tower 1 recycling waste water recycling waste water pump 7 introduced bottom falling-film evaporator 2 after, and part evaporation produces low temperature secondary steam in pipe; Low temperature secondary steam and recycling waste water flow into separate chamber in the lump, and the low temperature secondary steam after gas-liquid separation sends into compressor 4;
4) low temperature secondary steam boil down to pressure is 0.14 ~ 0.6MPa (A) by compressor 4, and the high-temperature high-pressure overheat steam that temperature is 110 ~ 220 DEG C also sends into the supplementary steam of desorption tower 1 as heating steam.
The desorption gas temperature that desorb tower top is discharged is 95 ~ 135 DEG C, and condensing rear ammonia stripping temperature is 90 ~ 115 DEG C, and hot wastewater temperature at the bottom of desorption tower is 98 ~ 155 DEG C, and the low temperature secondary steam temperature produced in falling-film evaporator 2 heating tube is 75 ~ 110 DEG C.
For realizing a kind of device of coked waste water desorb waste water falling film evaporation technology, comprise by the desorption tower 1 of pipeline communication, falling-film evaporator 2 and compressor 4, the desorption gas outlet of described desorption tower 1 tower top connects the gas inlet of falling-film evaporator 2 heating chamber, the vapour outlet of falling-film evaporator 2 connects the steam-in of compressor 4, and the vapour outlet of compressor 4 connects supplementary steam-in bottom desorption tower 1; The ammonia vapor outlet of falling-film evaporator 2 connects coal gas system in addition, and the condensed liquid outlet of falling-film evaporator 2 connects tar stock sump 5; The recycling waste water entrance of falling-film evaporator 2 separator connects the hot wastewater outlet of desorption tower 1 bottom, bottom falling-film evaporator 2, separate chamber and overhead-liquid distribution apparatus connecting pipe establishes recycling waste water pump 7.
Described raw material sump 5 is provided with coked waste water entrance in addition, the coked waste water outlet of raw material sump 5 is communicated with desorption tower 1 top coked waste water entrance by raw material sump pump 8, sewage/wastewater heat exchange device 3, and sewage/wastewater heat exchange device 3 is communicated with hot wastewater outlet bottom desorption tower 1 additionally by waste water pump 6.
Following examples 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 are not limited to following embodiment.In following embodiment, method therefor is ordinary method if no special instructions.
[embodiment 1]
In the incoming stock sump 5 of coked waste water, after sending sewage/wastewater heat exchange device 3 and hot wastewater heat exchange to be warming up to 97 DEG C with raw material sump pump 8 extraction, send into desorption tower 1 top, in Ta Nei and upflowing vapor counter current contact, done in order to desorb wherein contained NH by heating, stripping
3, H
2the components such as S, HCN.
Gained hot wastewater temperature 105 DEG C after desorb, major part waste water pump 6 send biochemical operation to process further after sewage/wastewater heat exchange device 3 and coked waste water heat exchange are lowered the temperature, and small part hot wastewater enters the separate chamber of falling-film evaporator 2.The liquid distribution device that vaporizer 2 top delivered to by recycling waste water recycling waste water pump 7 bottom falling-film evaporator 2 forms uniform liquid film and enters heating tube, and in pipe part evaporation generation 0.085MPa (A), the low temperature secondary steam of 95 DEG C.
Low temperature secondary steam and recycling waste water flow into the separate chamber of falling-film evaporator 2 in the lump, and after this gas-liquid separation, steam enters compressor 4, by compressor 4 to its compressed action, become 0.15MPa (A), the superheated vapour of 125 DEG C.The superheated vapour that compressor 4 exports enters desorption tower 1 and heats upflowing vapor needed for tower reactor waste water generation desorb.
The heating chamber that desorption tower 1 pushes up the 0.12MPa (A) of generation, the desorption gas of 103 DEG C enters falling-film evaporator 2, is cooled to 99 DEG C while heating cycle waste water, forms the ammonia vapour of condensed liquid and ammonia density 15%.Ammonia vapour send coke oven gas system, and condensed liquid flows in raw material sump 5.
[embodiment 2]
In the incoming stock sump 5 of coked waste water, after sending sewage/wastewater heat exchange device 3 and hot wastewater heat exchange to be warming up to 98 DEG C with raw material sump pump 8 extraction, send into desorption tower 1 top, in Ta Nei and upflowing vapor counter current contact, done in order to desorb wherein contained NH by heating, stripping
3, H
2the components such as S, HCN.
Gained hot wastewater temperature 106 DEG C after desorb, major part waste water pump 6 send biochemical operation to process further after sewage/wastewater heat exchange device 3 and coked waste water heat exchange are lowered the temperature, and small part hot wastewater enters the separate chamber of falling-film evaporator 2.The liquid distribution device that vaporizer 2 top delivered to by recycling waste water recycling waste water pump 7 bottom falling-film evaporator 2 forms uniform liquid film and enters heating tube, and in pipe part evaporation generation 0.051MPa (A), the low temperature secondary steam of 82 DEG C.
Low temperature secondary steam and recycling waste water flow into the separate chamber of falling-film evaporator 2 in the lump, and after this gas-liquid separation, steam enters compressor 4, by compressor 4 to its compressed action, become 0.157MPa (A), the superheated vapour of 135 DEG C.The superheated vapour that compressor exports enters desorption tower 1 and heats upflowing vapor needed for tower reactor waste water generation desorb.
The heating chamber that desorption tower 1 pushes up the 0.125MPa (A) of generation, the desorption gas of 103.5 DEG C enters falling-film evaporator 2, is cooled to 98 DEG C while heating cycle waste water, forms the ammonia vapour of condensed liquid and ammonia density 15.2%.Ammonia vapour send coke oven gas system, and condensed liquid flows in raw material sump 5.
[embodiment 3]
In the incoming stock sump 5 of coked waste water, after sending sewage/wastewater heat exchange device 3 and hot wastewater heat exchange to be warming up to 106 DEG C with raw material sump pump 8 extraction, send into desorption tower 1 top, in Ta Nei and upflowing vapor counter current contact, done in order to desorb wherein contained NH by heating, stripping
3, H
2the components such as S, HCN.
Gained hot wastewater temperature 114 DEG C after desorb, major part waste water pump 6 send biochemical operation to process further after sewage/wastewater heat exchange device 3 and coked waste water heat exchange are lowered the temperature, and small part hot wastewater enters the separate chamber of falling-film evaporator 2.The liquid distribution device that vaporizer 2 top delivered to by recycling waste water recycling waste water pump 7 bottom falling-film evaporator 2 forms uniform liquid film and enters heating tube, and in pipe part evaporation generation 0.096MPa (A), the low temperature secondary steam of 98 DEG C.
Low temperature secondary steam and recycling waste water flow into the separate chamber of falling-film evaporator 2 in the lump, and after this gas-liquid separation, steam enters compressor 4, by compressor 4 to its compressed action, become 0.19MPa (A), the superheated vapour of 142 DEG C.The superheated vapour that compressor 4 exports enters desorption tower 1 and heats upflowing vapor needed for tower reactor waste water generation desorb.
The heating chamber that desorption tower 1 pushes up the 0.15MPa (A) of generation, the desorption gas of 108 DEG C enters falling-film evaporator 2, is cooled to 105 DEG C while heating cycle waste water, forms the ammonia vapour of condensed liquid and ammonia density 18%.Ammonia vapour send coke oven gas system, and condensed liquid flows in raw material sump 5.
Claims (4)
1. a coked waste water desorb waste water falling film evaporation technology, is characterized in that, comprise the steps:
1) coked waste water after heat exchange enters desorption tower top, and heating steam enters at the bottom of desorption tower, the NH in coked waste water
3, H
2the components such as S, HCN desorption gas after steam stripped desorb is discharged by tower top;
2) desorption gas of discharging from desorb tower top enters the heating chamber of falling-film evaporator, and the part hot wastewater at the bottom of desorption tower enters the separate chamber of falling-film evaporator, forms ammonia vapour and the condensed liquid that ammonia density is 10 ~ 20% after desorption gas and wastewater heat exchange; 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 pumping sewage/wastewater heat exchange device, enters desorption tower top with after the hot wastewater heat exchange of being extracted out at the bottom of desorption tower by waste water pump; Waste water after heat exchange cooling send biochemical operation to process further;
3) enter heating tube be pumped to the liquid distribution device formation uniform liquid film at falling-film evaporator top from the desorption tower recycling waste water recycling waste water introduced bottom falling-film evaporator after, and part evaporation produces low temperature secondary steam in pipe; Low temperature secondary steam and recycling waste water flow into separate 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 ~ 0.6MPa (A) by compressor, and the high-temperature high-pressure overheat steam that temperature is 110 ~ 220 DEG C also sends into the supplementary steam of desorption tower as heating steam.
2. a kind of coked waste water desorb waste water falling film evaporation technology according to claim 2, it is characterized in that, the desorption gas temperature that desorb tower top is discharged is 95 ~ 135 DEG C, condensing rear ammonia stripping temperature is 90 ~ 115 DEG C, hot wastewater temperature at the bottom of desorption tower is 98 ~ 155 DEG C, and the low temperature secondary steam temperature produced in falling-film evaporator heating tube is 75 ~ 110 DEG C.
3. for realizing the device of a kind of coked waste water desorb waste water falling film evaporation technology according to claim 1, it is characterized in that, comprise by the desorption tower of pipeline communication, falling-film evaporator and compressor, the desorption gas outlet of described desorption tower tower top connects the gas inlet of falling-film evaporator heating chamber, the vapour outlet of falling-film evaporator connects the steam-in of compressor, and the vapour outlet of compressor connects supplementary steam-in bottom desorption tower; The ammonia vapor outlet of falling-film evaporator connects coal gas system in addition, 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 wastewater outlet of desorption tower bottom, bottom falling-film evaporator, separate chamber and overhead-liquid distribution apparatus connecting pipe establishes recycling waste water pump.
4. a kind of coked waste water desorb waste water falling film evaporation device according to claim 3, it is characterized in that, described raw material sump is provided with coked waste water entrance in addition, the coked waste water outlet of raw material sump is communicated with desorption tower top coked waste water entrance by raw material sump pump, sewage/wastewater heat exchange device, and sewage/wastewater heat exchange device is communicated with hot wastewater outlet bottom desorption tower additionally by waste water pump.
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 |
Applications Claiming Priority (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 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104986816A true CN104986816A (en) | 2015-10-21 |
| CN104986816B CN104986816B (en) | 2017-01-11 |
Family
ID=54298745
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510084437.2A Expired - Fee Related CN104986816B (en) | 2015-02-16 | 2015-02-16 | Process and apparatus for carrying out wastewater desorption and falling film evaporation on coking sewage |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104986816B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105906123A (en) * | 2016-05-26 | 2016-08-31 | 苏州派宁环保科技有限公司 | Chemical wastewater treatment system and method based on steam stripping and MVR combined process |
| CN108069479A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of wastewater treatment method and system |
| CN108069482A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of waste water treatment process and system |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN102671510A (en) * | 2011-11-29 | 2012-09-19 | 中国石油化工股份有限公司 | 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 |
-
2015
- 2015-02-16 CN CN201510084437.2A patent/CN104986816B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN102671510A (en) * | 2011-11-29 | 2012-09-19 | 中国石油化工股份有限公司 | 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 |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105906123A (en) * | 2016-05-26 | 2016-08-31 | 苏州派宁环保科技有限公司 | Chemical wastewater treatment system and method based on steam stripping and MVR combined process |
| 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 |
| CN108069479A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of wastewater treatment method and system |
| CN108069482A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of waste water treatment process and system |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104986816B (en) | 2017-01-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104788289B (en) | A kind of pump coupled heat technique of ethylene glycol rectifying | |
| CN102659196A (en) | Energy-saving evaporation process and system thereof | |
| CN101558037B (en) | Process for urea production and related plant | |
| CN102336415B (en) | Tubular furnace negative pressure ammonia distillation process | |
| CN107619078B (en) | Device for treating acidic wastewater by adopting concentration stripping method | |
| CN102190341A (en) | Stripping ammonia-removing method based on flash evaporation and heat pump technologies | |
| CN102241418A (en) | Negative pressure distillation equipment and method for residual ammonia water | |
| CN106348368A (en) | Heat pump evaporation system and heat pump evaporation method used for processing low-activity liquid waste in nuclear plant | |
| CN104817481A (en) | Technological method for recovering DMSO from DMSO aqueous solution | |
| CN104986816B (en) | Process and apparatus for carrying out wastewater desorption and falling film evaporation on coking sewage | |
| CN101591269A (en) | Improving one's methods of urea production equipment | |
| CN204625230U (en) | A kind of coked waste water desorb waste water falling film evaporation device | |
| CN104724776A (en) | Device and method for mixing secondary steam into pressurized water in pressurized evaporation | |
| CN108083984A (en) | For glyphosate solvent and the method for by-product recovery | |
| CN104058475A (en) | Novel heat pump distillation deamination energy-saving process | |
| CN204151096U (en) | A kind of industry contains pre-treatment and the heat reclamation device of ammonia sewage | |
| CN116751613A (en) | Energy-saving negative pressure debenzolization process and system | |
| CN106745062A (en) | The technique and device of a kind of negative-pressure operation production concentrated ammonia liquor | |
| CN115978519A (en) | Gasification slag water waste heat recovery system | |
| CN113175664B (en) | Recycling device and method for mixed working medium of feed water heating system | |
| CN104829032A (en) | Ammonia-nitrogen wastewater treatment system | |
| CN106500086B (en) | A kind of exhaust steam recycling and recovery system | |
| CN102442884B (en) | Method for recovering ethanol during soy production process and device thereof | |
| RU2528452C2 (en) | Method of heating at steam heat exchangers and plant to this end | |
| CN108190838B (en) | Hydrogen fluoride multiphase gasification separation recovery system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
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 |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170111 |