CN204251405U - A kind of Novel supercritical Water oxidize total system - Google Patents
A kind of Novel supercritical Water oxidize total system Download PDFInfo
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- CN204251405U CN204251405U CN201420758867.9U CN201420758867U CN204251405U CN 204251405 U CN204251405 U CN 204251405U CN 201420758867 U CN201420758867 U CN 201420758867U CN 204251405 U CN204251405 U CN 204251405U
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 239000012530 fluid Substances 0.000 claims abstract description 31
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000011084 recovery Methods 0.000 claims abstract description 18
- 239000002918 waste heat Substances 0.000 claims abstract description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000001301 oxygen Substances 0.000 claims abstract description 12
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 12
- 150000003839 salts Chemical class 0.000 claims abstract description 11
- 238000001704 evaporation Methods 0.000 claims abstract description 10
- 230000008020 evaporation Effects 0.000 claims abstract description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 9
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 9
- 239000002994 raw material Substances 0.000 claims abstract description 9
- 238000009284 supercritical water oxidation Methods 0.000 claims abstract description 8
- 235000011089 carbon dioxide Nutrition 0.000 claims abstract description 5
- 238000010612 desalination reaction Methods 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 45
- 238000005057 refrigeration Methods 0.000 claims description 25
- 238000010521 absorption reaction Methods 0.000 claims description 22
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 238000006297 dehydration reaction Methods 0.000 claims description 8
- 230000018044 dehydration Effects 0.000 claims description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical group N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 6
- 230000001590 oxidative effect Effects 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 239000007800 oxidant agent Substances 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 9
- 238000004064 recycling Methods 0.000 abstract description 5
- 239000006227 byproduct Substances 0.000 abstract description 2
- 230000008021 deposition Effects 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 8
- 238000000034 method Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 239000010815 organic waste Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 229910017053 inorganic salt Inorganic materials 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000009303 advanced oxidation process reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The utility model relates to a kind of Novel supercritical Water oxidize total system, and it comprises as lower unit: (1). oxygenant feeding unit; (2). raw material supply unit; (3). supercritical water oxidation desalination unit; (4). pressure energy recovery unit; (5). waste heat recovery unit; (6). carbonic acid gas output unit; (7). vaporize water output unit.Raw material of the present utility model and vaporize water Pipeline transport be the fluid of undercritical conditions, salt deposit is there will not be to cause line clogging, adopt reverse-flow evaporation wall reactor, its evaporation wall structure avoids the deposition of salts substances at reactor wall, reduces corrodibility; Waste heat and pressure energy are obtained for recycling, oxygen enrichment recycling tail gas, reduce the cost of operation; The food-grade carbon-dioxide of by-product and saturation steam are sold and also can be expanded income.
Description
Technical field
The utility model relates to the supercritical sewage treatment reactor of environmental technology field, particularly a kind of Novel supercritical Water oxidize total system.
Background technology
Supercritical water oxidation (SCWO) technology be the earliest 20th century the mid-80 proposed by American scholar Modell can fully, up hill and dale by advanced oxidation processes that organic constitution destroys.Point out in one of listed by American National gordian technique six large fields " energy and environment ", the most promising waste treatment technique is SCWO method.
Supercritical water (SCW) refers to that temperature is more than 374.15 DEG C, pressure is more than the water of the special state of 22.12Mpa, the dielectric coefficient of this Water Under reduces greatly, oxygen and gas chromatography matter form homogeneous phase in aqueous systems, eliminate resistance to mass transfer, make the heterogeneous reaction originally occurred between liquid phase, solid phase, gas phase be converted into the homogeneous oxidizing reaction in SCW, speed of reaction is faster, and the residence time is shorter.And scarcely need to use catalyzer, oxidation efficiency is very high, and most of organic clearance can reach more than 99%.In addition, inorganic component and salt solubleness in SCW is very low, almost can Precipitation completely, makes the separation of salt in reaction process become easy.When organic concentration is at 1wt% ~ 2wt%, the oxidation heat liberation of self just can be relied in reaction process to maintain the temperature needed for reaction, and do not need extraneous heat supply, unnecessary heat energy can reclaim.Because reaction is carried out under the environment closed, meet the requirement of totally-enclosed process.Temperature of reaction is far below burning, and the generation of non-secondary pollution thing.
At present, in most of supercritical water oxidation technique, waste water and oxidant fluid are preheating to super critical condition in advance and then enter reactor, ensure the carrying out reacted.But the salt sedimentation occurred in pre-heating stage and reactor like this can cause serious line clogging and material corrosion, a lot of equipment is difficult to the operation of held stationary, greatly constrains the development of this technology.In addition, the high running cost that oxygen, hydrogen peroxide etc. bring as oxygenant, also anxious to be resolved.
Summary of the invention
The purpose of this utility model is to overcome the deficiencies in the prior art, one is provided effectively to overcome line clogging and reactor corrosion, and waste heat recovery and pressure recoverable Novel supercritical Water oxidize total system can be realized, this system is by reclaiming End gas production food-grade carbon-dioxide, and from tail gas, isolate oxygen-rich oxide agent reuse, thus reduce system operation cost.
The utility model solves its technical problem and is achieved through the following technical solutions:
A kind of Novel supercritical Water oxidize total system, is characterized in that: comprise as lower unit:
(1). oxygenant feeding unit: be connected with the oxidant inlet of reactor after being connected successively by oxygenant storage tank, topping-up pump, oxygenant electric heater;
(2). raw material supply unit: be connected with reactor content entrance after being connected successively by liquid high pressure volume pump, first-class heat exchanger, startup electric heater;
(3). supercritical water oxidation desalination unit: comprise reactor, reactor bottom is shaped with salt outlet, reactor top is shaped with supercutical fluid outlet, supercutical fluid outlet connects the first-class heat exchanger of series connection, secondary heat exchanger and three grades of interchanger, arrange back pressure valve three grades of exchanger heat fluid outlet positions;
(4). pressure energy recovery unit: comprise one-level hydraulic turbine unit, the first gas-liquid separator, secondary hydraulic turbine unit, the 3rd diverting valve connecting successively, one-level hydraulic turbine unit inlet is connected with the hot fluid outlet ports of three grades of interchanger, and the hot fluid outlet ports of secondary hydraulic turbine unit is connected with the 3rd diverting valve;
(5). waste heat recovery unit: comprise the 3rd interchanger, the second diverting valve and absorption refrigeration device, the fluid that the 3rd diverting valve separates is leaded up to three grades of interchanger and is carried out waste heat recovery, and another road is connected to water purifying tank; 3rd interchanger connects the second diverting valve, and the second diverting valve connects absorption refrigeration device, and for it provides thermal source, the second diverting valve also connects a steam product outlet;
(6). carbonic acid gas output unit: comprise the dehydration tower, water cooling heat exchanger, rectifying tower, absorption refrigeration device and the second gas-liquid separator that connect successively, first gas-liquid separator pneumatic outlet connects dehydration tower, and the second gas-liquid separator connects food-grade carbon-dioxide relief outlet and oxygen, nitrogen relief outlet;
(7). vaporize water output unit: comprise water purifying tank, liquid high pressure volume pump, secondary heat exchanger, first diverting valve of connecting successively, the 3rd diverting valve and absorption refrigeration device are all connected to water purifying tank, and the first diverting valve is connected to reactor.
And described reactor is reverse-flow evaporation wall reactor.
And described first-class heat exchanger, secondary heat exchanger, three grades of interchanger are shell and tube heat exchanger.
And the first described gas-liquid separator, the second gas-liquid separator top are provided with demister and back pressure valve, and bottom is provided with Liquid level valve.
And described absorption refrigeration device is ammonia absorption type refrigeration device or lithium bromide absorbing type refrigeration device.
Advantage of the present utility model and beneficial effect are:
Raw material of the present utility model and vaporize water Pipeline transport be the fluid of undercritical conditions, salt deposit is there will not be to cause line clogging, adopt reverse-flow evaporation wall reactor, its evaporation wall structure avoids the deposition of salts substances at reactor wall, reduces corrodibility; Waste heat and pressure energy are obtained for recycling, oxygen enrichment recycling tail gas, reduce the cost of operation; The food-grade carbon-dioxide of by-product and saturation steam are sold and also can be expanded income.
Accompanying drawing explanation
Fig. 1 is Novel supercritical Water oxidize total system process flow sheet.
Description of reference numerals:
1-oxygenant storage tank, 2-topping-up pump, the reverse-flow evaporation wall reactor of 3-, 4-first diverting valve, 5-tri-grades of interchanger, 6-water cooling heat exchanger, 7-rectifying tower, 8-second diverting valve, 9-absorption refrigeration device, 10-second gas-liquid separator, 11-one-level hydraulic turbine unit, 12-first gas-liquid separator, 13-secondary hydraulic turbine unit, 14-the 3rd diverting valve, 15-secondary heat exchanger, 16-first-class heat exchanger, 17-water purifying tank, 18-first liquid high-pressure metering pump, 19-second liquid high-pressure metering pump, 20-oxygenant electric heater, 21-starts electric heater, 22-dehydration tower.
Embodiment
Below by specific embodiment, the utility model is described in further detail, and following examples are descriptive, is not determinate, can not limit protection domain of the present utility model with this.
A kind of Novel supercritical Water oxidize total system, it comprises as lower unit:
(1). oxygenant feeding unit: be connected with the oxidant inlet of reactor 3 after being connected successively by oxygenant storage tank 1, topping-up pump 2, oxygenant electric heater 20.
(2). raw material supply unit: be connected with reactor content entrance after connecting successively by first liquid high-pressure metering pump 18, first-class heat exchanger 16, startup electric heater 21.
(3). supercritical water oxidation desalination unit: comprise reactor, reactor is reverse-flow evaporation wall reactor.Reactor bottom is shaped with salt outlet, and reactor top is shaped with supercutical fluid outlet, and supercutical fluid outlet connects series connection first-class heat exchanger, and secondary heat exchanger 15 and three grades of interchanger 5, arrange back pressure valve three grades of exchanger heat fluid outlet positions; First-class heat exchanger, secondary heat exchanger, three grades of interchanger are shell and tube heat exchanger.
(4). pressure energy recovery unit: comprise one-level hydraulic turbine unit 11, first gas-liquid separator 12, secondary hydraulic turbine unit the 13, the 3rd diverting valve 14 of connecting successively, one-level hydraulic turbine unit inlet is connected with the hot fluid outlet ports of three grades of interchanger, and the hot fluid outlet ports of secondary hydraulic turbine unit is connected with the 3rd diverting valve; First gas-liquid separator top is provided with demister and back pressure valve, and bottom is provided with Liquid level valve.
(5). waste heat recovery unit: comprise fluid that the 3rd interchanger, the second diverting valve 8 and absorption refrigeration device the 9, three diverting valve separate and lead up to three grades of interchanger and carry out waste heat recovery, another road is connected to water purifying tank; 3rd interchanger connects the second diverting valve, and the second diverting valve connects absorption refrigeration device, and for it provides thermal source, the second diverting valve also connects a steam product outlet.Absorption refrigeration device is ammonia absorption type refrigeration device or lithium bromide absorbing type refrigeration device.
(6). carbonic acid gas output unit: comprise the dehydration tower 22, water cooling heat exchanger 6, rectifying tower 7, absorption refrigeration device and the second gas-liquid separator 10 that connect successively, first gas-liquid separator pneumatic outlet connects dehydration tower, and the second gas-liquid separator connects food-grade carbon-dioxide relief outlet and oxygen, nitrogen relief outlet.Second gas-liquid separator top is provided with demister and back pressure valve, and bottom is provided with Liquid level valve.
(7). vaporize water output unit: comprise water purifying tank 17, second liquid high-pressure metering pump 19, secondary heat exchanger, the first diverting valve the 4, three diverting valve and the absorption refrigeration device of connecting successively and be all connected to water purifying tank, the first diverting valve is connected to reactor.
The principle of work of Novel supercritical Water oxidize total system of the present utility model is:
(1). oxygenant supply: oxygenant through topping-up pump supercharging, and is supplied to the oxidant inlet of reactor after the heating of oxygenant electric heater, and the temperature of the oxygenant after supercharging, heating controls at 300-370 DEG C, and pressure-controlling is at 22-35Mpa.
(2). raw material supply: organic waste are supplied to reactor content entrance successively after the pressurization of liquid high pressure volume pump, first-class heat exchanger heating, the heating of startup electric heater, organic waste raw material temperature after pressurization, heat exchange controls at 300-370 DEG C, and pressure-controlling is at 22-35Mpa.
(3). supercritical water oxidation desalination unit: after oxygenant and organic waste enter reactor, mixed firing, produce supercutical fluid and insoluble inorganic salt, inorganic salt and a small amount of liquid water are discharged from the salt outlet of reactor bottom, and supercutical fluid is discharged from the supercutical fluid outlet on reactor top; Supercutical fluid successively with first-class heat exchanger, secondary heat exchanger and three grades of interchanger carry out heat exchange.It is heating raw materials that supercutical fluid exports out by first-class heat exchanger from supercutical fluid, and the fluid after heat exchange still has very large heat, can again by secondary heat exchanger be vaporize water heating, unnecessary heat produces 160 DEG C of saturation steams by three grades of interchanger 5.
(4). pressure energy reclaims: through the hot-fluid of three grades of interchanger successively through one-level hydraulic turbine unit, the first gas-liquid separator and secondary hydraulic turbine unit, the hot fluid outlet ports of secondary hydraulic turbine unit is connected to the 3rd diverting valve.From three grades of interchanger high pressure fluid out first through hydraulic turbine unit, pressure recovery energy, control the first gas-liquid separator top back pressure valve, pressure-controlling is at 5-10Mpa.From the liquid that the first gas-liquid separator is discharged, still there is very high pressure, the further pressure recovery energy of available second hydraulic turbine unit, from the second hydraulic turbine unit water purification out, there is higher heat, 40-60% divides diffluence to produce the saturation steam of 160 DEG C, all the other blended absorbent refrigerators hot water out enters water purifying tank, hot water in water purifying tank has very high heat, can use as heating and heat supply completely, meanwhile, vaporize water is from extracting here, in secondary heat exchanger heat exchange after the pressurization of liquid high pressure volume pump, after shunting, enter reactor.
(5). waste heat recovery: distribute the saturation steam of 40-60% water by producing >150 DEG C after three grades of interchanger from the 3rd diverting valve, recovery waste heat, rest part enters water purifying tank; Saturation steam distributes 5-10% saturation steam by the second diverting valve again and enters absorption refrigeration device and provide thermal source for it, and produce the cooling medium water of <-25 DEG C, rest part is steam product.
(6). carbonic acid gas output: the first gas-liquid separator is by back pressure valve control pressure 5-10Mpa, the gas phase produced is dewatered through dehydration tower, rectifying tower is entered again after water cooling heat exchanger is cooled to 20-30 DEG C, be separated through rectifying tower and obtain liquid carbon dioxide and oxygen-containing gas, oxygen-containing gas gets back to oxygenant storage tank, realize oxygen recovery, liquid carbon dioxide cools to <-25 DEG C further by absorption refrigeration device, enter the second gas-liquid separator again, control pressure of the gas and liquid separator 2-5Mpa and carry out reducing pressure by regulating flow, parse the oxygen of dissolving, nitrogen purge, obtain food-grade carbon-dioxide simultaneously.
(7). vaporize water output unit: in pressure energy recycling step, water through the 3rd diverting valve shunting enters water purifying tank, for absorption refrigeration device provides the cooling medium water after heat also to enter water purifying tank in waste heat recovery step, after the pressurization of liquid high pressure volume pump, again through secondary heat exchanger heat exchange, and become evaporation wall water and enter reactor after the first diverting valve shunting, evaporation wall water controls at 22-35Mpa, 200-370 DEG C after pressurization and heat exchange.
Although disclose embodiment of the present utility model and accompanying drawing for the purpose of illustration, but it will be appreciated by those skilled in the art that: in the spirit and scope not departing from the utility model and claims, various replacement, change and amendment are all possible, therefore, scope of the present utility model is not limited to the content disclosed in embodiment and accompanying drawing.
Claims (5)
1. a Novel supercritical Water oxidize total system, is characterized in that: comprise as lower unit:
(1). oxygenant feeding unit: be connected with the oxidant inlet of reactor after being connected successively by oxygenant storage tank, topping-up pump, oxygenant electric heater;
(2). raw material supply unit: be connected with reactor content entrance after being connected successively by liquid high pressure volume pump, first-class heat exchanger, startup electric heater;
(3). supercritical water oxidation desalination unit: comprise reactor, reactor bottom is shaped with salt outlet, reactor top is shaped with supercutical fluid outlet, supercutical fluid outlet connects the first-class heat exchanger of series connection, secondary heat exchanger and three grades of interchanger, arrange back pressure valve three grades of exchanger heat fluid outlet positions;
(4). pressure energy recovery unit: comprise one-level hydraulic turbine unit, the first gas-liquid separator, secondary hydraulic turbine unit, the 3rd diverting valve connecting successively, one-level hydraulic turbine unit inlet is connected with the hot fluid outlet ports of three grades of interchanger, and the hot fluid outlet ports of secondary hydraulic turbine unit is connected with the 3rd diverting valve;
(5). waste heat recovery unit: comprise the 3rd interchanger, the second diverting valve and absorption refrigeration device, the fluid that the 3rd diverting valve separates is leaded up to third stage interchanger and is carried out waste heat recovery, and another road is connected to water purifying tank; 3rd interchanger connects the second diverting valve, and the second diverting valve connects absorption refrigeration device, and for it provides thermal source, the second diverting valve also connects a steam product outlet;
(6). carbonic acid gas output unit: comprise the dehydration tower, water cooling heat exchanger, rectifying tower, absorption refrigeration device and the second gas-liquid separator that connect successively, first gas-liquid separator pneumatic outlet connects dehydration tower, and the second gas-liquid separator connects food-grade carbon-dioxide relief outlet and oxygen, nitrogen relief outlet;
(7). vaporize water output unit: comprise water purifying tank, liquid high pressure volume pump, secondary heat exchanger, first diverting valve of connecting successively, the 3rd diverting valve and absorption refrigeration device are all connected to water purifying tank, and the first diverting valve is connected to reactor.
2. Novel supercritical Water oxidize total system according to claim 1, is characterized in that: described reactor is reverse-flow evaporation wall reactor.
3. Novel supercritical Water oxidize total system according to claim 1, is characterized in that: described first-class heat exchanger, secondary heat exchanger, three grades of interchanger are shell and tube heat exchanger.
4. Novel supercritical Water oxidize total system according to claim 1, is characterized in that: the first described gas-liquid separator, the second gas-liquid separator top are provided with demister and back pressure valve, and bottom is provided with Liquid level valve.
5. Novel supercritical Water oxidize total system according to claim 1, is characterized in that: described absorption refrigeration device is ammonia absorption type refrigeration device or lithium bromide absorbing type refrigeration device.
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| CN201420758867.9U CN204251405U (en) | 2014-12-05 | 2014-12-05 | A kind of Novel supercritical Water oxidize total system |
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| CN201420758867.9U CN204251405U (en) | 2014-12-05 | 2014-12-05 | A kind of Novel supercritical Water oxidize total system |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445573A (en) * | 2014-12-05 | 2015-03-25 | 内蒙古天一环境技术有限公司 | Novel supercritical water oxidation comprehensive treatment system and method |
| CN106495385A (en) * | 2016-12-01 | 2017-03-15 | 莫比森(北京)石油天然气技术开发有限公司 | A kind of supercritical oxidation method for processing waste water |
| CN110015747A (en) * | 2019-05-24 | 2019-07-16 | 山东豪迈化工技术有限公司 | Supercritical water oxidation apparatus and wastewater treatment method |
| CN111392912A (en) * | 2020-04-21 | 2020-07-10 | 江苏暻慧诚环境工程有限公司 | Oil-based cutting waste liquid treatment and separation system and working method thereof |
| US11565956B2 (en) * | 2018-11-09 | 2023-01-31 | Jiangsu Institute Of Environmental Science | Multifunctional continuous hydrothermal oxidation experiment system and use method therefor |
-
2014
- 2014-12-05 CN CN201420758867.9U patent/CN204251405U/en not_active Withdrawn - After Issue
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445573A (en) * | 2014-12-05 | 2015-03-25 | 内蒙古天一环境技术有限公司 | Novel supercritical water oxidation comprehensive treatment system and method |
| WO2016086741A1 (en) * | 2014-12-05 | 2016-06-09 | 王冰 | Novel supercritical water oxidation comprehensive processing system and processing method |
| CN106495385A (en) * | 2016-12-01 | 2017-03-15 | 莫比森(北京)石油天然气技术开发有限公司 | A kind of supercritical oxidation method for processing waste water |
| CN106495385B (en) * | 2016-12-01 | 2019-11-22 | 莫比森(北京)石油天然气技术开发有限公司 | A kind of supercritical oxidation method handling waste water |
| US11565956B2 (en) * | 2018-11-09 | 2023-01-31 | Jiangsu Institute Of Environmental Science | Multifunctional continuous hydrothermal oxidation experiment system and use method therefor |
| CN110015747A (en) * | 2019-05-24 | 2019-07-16 | 山东豪迈化工技术有限公司 | Supercritical water oxidation apparatus and wastewater treatment method |
| CN111392912A (en) * | 2020-04-21 | 2020-07-10 | 江苏暻慧诚环境工程有限公司 | Oil-based cutting waste liquid treatment and separation system and working method thereof |
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Owner name: WANG BING Free format text: FORMER OWNER: INNER MONGOLIA?TIANYI ENVIRONMENTAL?TECHNOLOGY?CO., LTD. Effective date: 20150605 |
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| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20150605 Address after: 010011 the Inner Mongolia Autonomous Region Ruyi Development Zone, Hohhot city building, No. 1207 Patentee after: Wang Bing Address before: 010011 the Inner Mongolia Autonomous Region Ruyi Development Zone, Hohhot city building, No. 1207 Patentee before: Inner Mongolia Tianyi Environmental Technology Co., Ltd. |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20150408 Effective date of abandoning: 20160608 |
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| C25 | Abandonment of patent right or utility model to avoid double patenting |