CN107915308A - The wet oxidation processing method of high concentrated organic wastewater - Google Patents
The wet oxidation processing method of high concentrated organic wastewater Download PDFInfo
- Publication number
- CN107915308A CN107915308A CN201610880370.8A CN201610880370A CN107915308A CN 107915308 A CN107915308 A CN 107915308A CN 201610880370 A CN201610880370 A CN 201610880370A CN 107915308 A CN107915308 A CN 107915308A
- Authority
- CN
- China
- Prior art keywords
- wet oxidation
- catalyst
- processing method
- oxidation processing
- waste water
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
Abstract
The present invention relates to the wet oxidation processing method of high concentrated organic wastewater.To solve the problems, such as that the COD efficiency in existing catalyst degradation waste water is low.Wet oxidation processing method of the invention by using high concentrated organic wastewater, in the presence of wet oxidation heterogeneous catalyst, the waste water and oxygenous oxidant are reacted to the reducing substances removed in waste water in the reactor, the wet oxidation heterogeneous catalyst, in parts by weight, including following components：(1) 90~99.5 part of catalyst carrier；(2) 0.1~5 parts of technical solutions selected from least one of platinum family noble metal, preferably solve the problems, such as this, available for the organic matter in fast degradation high concentrated organic wastewater.
Description
Technical field
The present invention relates to the wet oxidation processing method of high concentrated organic wastewater.
Technical background
Industry high-concentration organic wastewater COD value is often higher than 2000mg/L, and some is even as high as ten tens of thousands of mg/L.Such is useless
For water containing poisonous and harmful compounds such as aldehyde, phenol, amine, acid, biodegradable performance is low, very big to environmental hazard.Catalytic wet oxidation
It is a kind of platform technology for handling middle and high concentration organic wastewater.Its main feature is that organic wastewater is in high temperature (125~320 DEG C), high pressure
Under the conditions of (0.5~20MPa), using air or pure oxygen as oxidant, under the action of catalyst, by organic pollution oxygen in liquid phase
Turn to CO2With inorganic matter or the small organic molecule such as water.The technique is a kind of method for processing organic wastewater of energy-saving and environment friendly,
It is highly suitable for the processing of high concentrated organic wastewater.
CN1631818 disclosure of the invention a kind of organic wastewater treatment process, its step include：Materialized pretreatment, anaerobism water
Solve acidification and the processing of TCBS systems.The invention can improve the biodegradability of organic wastewater, strengthening system resistance to poison with it is resistance to
Impact, consolidation system biological denitrificaion function, by cut down that pollutional load makes organic wastewater step by step reach national requirements for environmental protection.
But this method is only applicable to processing low-concentration organic waste water.
CN101553436, which is disclosed a kind of device for being used to handle high concentrated organic wastewater and handled using the device, to be had
The method of machine waste water.Device for handling high concentrated organic wastewater includes carrier reactor, which, which receives, waits to locate
The organic wastewater of reason, and it is included in come oxygenolysis using the aerobe for being attached to carrier organic material in organic wastewater
Material.But this method is not suitable for handling the organic wastewater containing bio-toxicity.
CN102125842 discloses a kind of preparation method of multiphase wet oxidation catalyst.With selected from platinum, ruthenium, rhodium, iridium,
One or more of precious metal elements in gold are active component；With the one kind or several of rare earth element in lanthanum, cerium, praseodymium, neodymium
The rare earth element of kind is helper component；Active component and helper component are supported and contained in ceramic-absorbent charcoal carrier, wherein activated carbon
Measure as the 1~15% of the ceramic-absorbent charcoal total weight of carrier, and in active component and helper component every kind of element weight it is each
From accounting for the 0.25~5% of activated carbon weight.But due to using ceramic-absorbent charcoal, for carrier, carrier and active component exist this method
Easily it is lost under harsh reaction condition, therefore the catalyst, in long-term operation, COD removal efficiencies gradually reduce.
The content of the invention
The technical problems to be solved by the invention are that the efficiency of wet oxidizing catalyst removing COD of the prior art is low
Problem, there is provided a kind of wet oxidation processing method of new high concentrated organic wastewater, this method, which has, removes the efficient of COD
Advantage.
In order to solve the above technical problems, technical scheme is as follows：
The wet oxidation processing method of high concentrated organic wastewater, in the presence of wet oxidation heterogeneous catalyst, by described in
Waste water and oxygenous oxidant react the reducing substances removed in waste water, the wet oxidation heterogeneous catalysis in the reactor
Agent, in parts by weight, including following components：
(1) 90~99.5 part of catalyst carrier；
(2) 0.1~5 parts selected from least one of platinum family noble metal.
In above-mentioned technical proposal, the oxidant is preferably air or oxygen.
In above-mentioned technical proposal, the temperature of reaction is preferably 180~300 DEG C.
In above-mentioned technical proposal, reaction pressure is preferably 3~10MPa.
In above-mentioned technical proposal, the residence time of waste water is preferably 10~120 minutes.
In above-mentioned technical proposal, the catalyst carrier preferably is selected from TiO2、ZrO2、SiO2And Al2O3In one kind.
In above-mentioned technical proposal, the noble metal preferably is selected from least one of Ru, Pd, Pt, Ir and Rh.
In above-mentioned technical proposal, the catalyst has comparable effect to any concentration organic wastewater, but to high concentration
The processing of organic wastewater more has obvious advantage.The COD value of the high concentrated organic wastewater is preferably 10,000~200,
000mg/L。
In above-mentioned technical proposal, the catalyst preferably further includes (3) 0.1~5 parts of indiums, and the noble metal is being gone with indium
There is cooperative effect in terms of except the COD in waste water.
In above-mentioned technology, the wet oxidation heterogeneous catalyst can use the preparation method included the following steps to prepare：
1) compound solution containing precious metal element is mixed with carrier；
2) the compound state noble metal for introducing step 1) is simple substance.
In above-mentioned technical proposal, when containing indium in the catalyst, the preparation method can be further, including：
(1) mixed aqueous solution of the compound containing noble metal and compound and containing indium is mixed with carrier；
(2) noble metal of compound state and indium are reduced to simple substance.
In above-mentioned technical proposal, most preferred preparation method, including：
(i) noble metal will be contained and compound water solution is mixed with carrier；
(ii) the compound state noble metal introduced in step (i) is obtained into catalyst precursor I for simple substance；
(iii) mixed aqueous solution of the compound containing indium is mixed with catalyst precursor I；
(iv) the compound state indium that step (iii) introduces is reduced to simple substance.
When using noble metal and reduction is first impregnated, then impregnating what indium restored program again and preparing catalyst,
Invention catalyst has unusual good technique effect in terms of COD is removed.
In above-mentioned technical proposal, the specific method of reduction is not particularly limited, as long as can be the active component of compound state also
Originally it was simple substance.For example, vapour phase reduction can be carried out to predecessor with gaseous reducing agent, the solution of reducing agent can also be used
Or liquid-phase reduction agent carries out liquid-phase reduction.The common gas that can include hydrogen of gaseous reducing agent, such as hydrogen, hydrogen-nitrogen
Gas gaseous mixture etc..The reducing agent of liquid-phase reduction can be hydrazine hydrate, formic acid or sodium formate etc..
In above-mentioned technical proposal, the compound of the active component is not particularly limited, such as, but not limited to ruthenium trichloride,
Palladium bichloride, chlorine palladium acid, chloroplatinic acid, radium chloride, indium nitrate etc..
It is described to urge when reduction uses the gas of hydrogen to carry out vapour phase reduction for gaseous reducing agent in above-mentioned technical proposal
Agent predecessor preferably first passes through drying, or can further comprise roasting, preferably 400~600 DEG C of the temperature of roasting, roasting when
Between be preferably 2~4.5 it is small when.
One skilled in the art will appreciate that when hydrogen is reduced for reducing agent, it is for safety preferred with volume basis
Hydrogen content is less than 5% hydrogen nitrogen mixture.
In above-mentioned technical proposal, when being reduced using hydrogen, reduction temperature is preferably 300~700 DEG C, further preferably
350~600 DEG C；When recovery time is preferably 1~5 small, it is further preferred 2.5~4.5 it is small when.
In above-mentioned technical proposal, air dosage is preferably 1~2 times of the air quality as needed for calculating original waste water COD value.
Technical solution using the present invention, the results showed that the A-04 catalyst of platiniferous and indium while preparation with the present invention,
It it is 250 DEG C, pressure 6.5MPa in reaction temperature, the residence time is under conditions of 20 minutes, and it is organic can effectively to reduce high concentration
The content of organics of waste water, after wet oxidation is handled, industrial acrylic acid wastewater COD value is down to from 63,500mg/L of raw water
23mg/L, achieves preferable technique effect.
Below by embodiment, the invention will be further elaborated, but these embodiments are not anyway to this hair
Bright scope is construed as limiting.
Embodiment
【Embodiment 1】
1st, catalyst preparation
In terms of weight proportion, ZrO2:Ru:In is 97:2:1 prepares catalyst A-01.
By 97 parts of ZrO2Catalyst carrier is impregnated in the RuCl equivalent to 2 parts of Ru at room temperature3With the In (NO of 1 part of In3)3Water
In solution overnight, (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after 80 DEG C of dryings
When, obtain catalyst A-01.The formula of catalyst is shown in Table 1.
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g A-01 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
【Embodiment 2】
1st, catalyst preparation
In terms of weight proportion, ZrO2:Pd:In is 97:2:1 prepares catalyst A-02.
By 97 parts of ZrO2Catalyst carrier is impregnated in the PdCl equivalent to 2 parts of Pd at room temperature2With the In (NO of 1 part of In3)3Water
In solution overnight, (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after 80 DEG C of dryings
When, obtain catalyst A-02.The formula of catalyst is shown in Table 1.
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g A-02 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
【Embodiment 3】
1st, catalyst preparation
In terms of weight proportion, ZrO2:Pt:In is 97:2:1 prepares catalyst A-03.
By 97 parts of ZrO2Catalyst carrier is impregnated in the H equivalent to 2 parts of Pt at room temperature2PtCl6With the In (NO of 1 part of In3)3Water
In solution overnight, (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after 80 DEG C of dryings
When, obtain catalyst A-03.The formula of catalyst is shown in Table 1.
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g A-03 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
【Embodiment 4】
1st, catalyst preparation
In terms of weight proportion, ZrO2:Pt:In is 97:2:1 prepares catalyst A-04.
By 97 parts of ZrO2Catalyst carrier is impregnated in the H equivalent to 2 parts of Pt at room temperature2PtCl6In aqueous solution overnight, 80 DEG C
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after drying, before obtaining catalyst
Body B-04.B-04 is impregnated in the In (NO equivalent to 1 part of In3)3In aqueous solution overnight, in 300 DEG C of hydrogen gas after 80 DEG C of dryings
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under atmosphere, catalyst A-04 is obtained.The formula of catalyst is shown in Table
1。
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g A-04 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
Compare from embodiment 3 and embodiment 4 as can be seen that the side that noble metal is impregnated and reduced respectively using priority with indium
Formula, obtained catalyst have unusual good effect in terms of COD is removed.
【Embodiment 5】
1st, catalyst preparation
In terms of weight proportion, ZrO2:Pt:In is 97:2:1 prepares catalyst A-05.
By 97 parts of ZrO2Catalyst carrier is impregnated in the In (NO equivalent to 1 part of In at room temperature3)3In aqueous solution overnight, 80 DEG C
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after drying, before obtaining catalyst
Body B-05.B-04 is impregnated in the H equivalent to 2 parts of Pt2PtCl6In aqueous solution overnight, in 300 DEG C of hydrogen gas after 80 DEG C of dryings
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under atmosphere, catalyst A-05 is obtained.The formula of catalyst is shown in Table
1。
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g A-05 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
【Embodiment 6】
1st, catalyst preparation
In terms of weight proportion, TiO2:Pt:In is 97:2:1 prepares catalyst A-06.
By 97 parts of TiO2Catalyst carrier is impregnated in the H equivalent to 2 parts of Pt at room temperature2PtCl6In aqueous solution overnight, 80 DEG C
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after drying, before obtaining catalyst
Body B-06.B-06 is impregnated in the In (NO equivalent to 1 part of In3)3In aqueous solution overnight, in 300 DEG C of hydrogen gas after 80 DEG C of dryings
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under atmosphere, catalyst A-06 is obtained.The formula of catalyst is shown in Table
1。
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g A-06 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
【Embodiment 7】
In terms of weight proportion, Al2O3:Pt:In is 97:2:1 prepares catalyst A-07.
By 97 parts of Al2O3Catalyst carrier is impregnated in the H equivalent to 2 parts of Pt at room temperature2PtCl6In aqueous solution overnight, 80 DEG C
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after drying, before obtaining catalyst
Body B-07.B-07 is impregnated in the In (NO equivalent to 1 part of In3)3In aqueous solution overnight, in 300 DEG C of hydrogen gas after 80 DEG C of dryings
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under atmosphere, catalyst A-07 is obtained.The formula of catalyst is shown in Table
1。
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g A-07 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
【Embodiment 8】
In terms of weight proportion, SiO2:Pt:In is 97:2:1 prepares catalyst A-08.
By 97 parts of SiO2Catalyst carrier is impregnated in the H equivalent to 2 parts of Pt at room temperature2PtCl6In aqueous solution overnight, 80 DEG C
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after drying, before obtaining catalyst
Body B-08.B-08 is impregnated in the In (NO equivalent to 1 part of In3)3In aqueous solution overnight, in 300 DEG C of hydrogen gas after 80 DEG C of dryings
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under atmosphere, catalyst A-08 is obtained.The formula of catalyst is shown in Table
1。
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g A-08 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
【Comparative example 1】
1st, catalyst preparation
In terms of weight proportion, ZrO2:Pt is 97:3 prepare catalyst D-01.
By 97 parts of ZrO2Catalyst carrier is impregnated in the H equivalent to 3 parts of Pt at room temperature2PtCl6In aqueous solution overnight, 80 DEG C
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after drying, catalyst D- is obtained
01.The formula of catalyst is shown in Table 1.
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g D-01 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
【Comparative example 2】
1st, catalyst preparation
In terms of weight proportion, ZrO2:In is 97:3 prepare catalyst D-02.
By 97 parts of ZrO2Catalyst carrier is impregnated in the In (NO equivalent to 3 parts of In at room temperature3)3In aqueous solution overnight, 80 DEG C
When (hydrogen content is 4% hydrogen nitrogen mixture) reduction 4 is small under 300 DEG C of hydrogen atmospheres after drying, catalyst D- is obtained
02.The formula of catalyst is shown in Table 1.
2nd, evaluating catalyst
Using industrial acrylic acid wastewater as raw material, the COD value of waste water is 63,500mg/L.Waste water after oxygen mix with passing through dress
It is filled with the 125mL fixed bed reactors of 120g D-02 catalyst.Reaction temperature in reactor is 250 DEG C, and pressure is
6.5MPa, residence time are 20 minutes.Reaction result is shown in Table 2.
The formula of 1. catalyst of table
| Embodiment | Catalyst | Catalyst formulation | Each component quality proportioning |
| Embodiment 1 | A-01 | ZrO2:Ru:In | 97:2:1 |
| Embodiment 2 | A-02 | ZrO2:Pd:In | 97:2:1 |
| Embodiment 3 | A-03 | ZrO2:Pt:In | 97:2:1 |
| Embodiment 4 | A-04 | ZrO2:Pt:In | 97:2:1 |
| Embodiment 5 | A-05 | ZrO2:Pt:In | 97:2:1 |
| Embodiment 6 | A-06 | TiO2:Pt:In | 97:2:1 |
| Embodiment 7 | A-07 | Al2O3:Pt:In | 97:2:1 |
| Embodiment 8 | A-08 | SiO2:Pt:In | 97:2:1 |
| Comparative example 1 | D-01 | ZrO2:Pt | 97:3 |
| Comparative example 2 | D-02 | ZrO2:In | 97:3 |
2. reaction result of table
Claims (9)
1. the wet oxidation processing method of high concentrated organic wastewater, will be described useless in the presence of wet oxidation heterogeneous catalyst
Water and oxygenous oxidant react the reducing substances removed in waste water, the wet oxidation heterogeneous catalysis in the reactor
Agent, in parts by weight, including following components：
(1) 90~99.5 part of catalyst carrier；
(2) 0.1~5 parts selected from least one of platinum family noble metal.
2. wet oxidation processing method according to claim 1, it is characterized in that the oxidant is air or oxygen.
3. wet oxidation processing method according to claim 1, it is characterized in that the temperature of reaction is 180~300 DEG C.
4. wet oxidation processing method according to claim 1, it is characterized in that reaction pressure is 3~10MPa.
5. wet oxidation processing method according to claim 1, it is characterized in that the residence time of waste water is 10~120 points
Clock.
6. wet oxidation processing method according to claim 1, it is characterized in that the catalyst carrier is selected from TiO2、
ZrO2、SiO2And Al2O3In one kind.
7. wet oxidation processing method according to claim 1, it is characterized in that the noble metal is selected from Ru, Pd, Pt, Ir
At least one of with Rh.
8. wet oxidation processing method according to claim 1, it is characterized in that the COD value of the high concentrated organic wastewater is
10,000~200,000mg/L.
9. the wet oxidation processing method described in claim 1, includes it is characterized in that the wet oxidation heterogeneous catalyst uses
It is prepared by the preparation method of following steps：
1) compound solution containing precious metal element is mixed with carrier；
2) the compound state noble metal for introducing step 1) is simple substance.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610880370.8A CN107915308A (en) | 2016-10-09 | 2016-10-09 | The wet oxidation processing method of high concentrated organic wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610880370.8A CN107915308A (en) | 2016-10-09 | 2016-10-09 | The wet oxidation processing method of high concentrated organic wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107915308A true CN107915308A (en) | 2018-04-17 |
Family
ID=61892358
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610880370.8A Pending CN107915308A (en) | 2016-10-09 | 2016-10-09 | The wet oxidation processing method of high concentrated organic wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107915308A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112441678A (en) * | 2019-09-03 | 2021-03-05 | 中国石油化工股份有限公司 | Method for treating saccharin production wastewater |
| CN112619665A (en) * | 2019-09-24 | 2021-04-09 | 中国石油化工股份有限公司 | Wet oxidation heterogeneous catalyst and preparation method thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59115786A (en) * | 1982-12-21 | 1984-07-04 | Osaka Gas Co Ltd | Wet oxidation treatment of waste water |
| US20040104181A1 (en) * | 2000-01-05 | 2004-06-03 | Yusuke Shiota | Catalyst for treating waste water, method for preparing the same and process for treating waste water |
| CN103420473A (en) * | 2012-05-16 | 2013-12-04 | 中国石油化工股份有限公司 | Processing method of wastewater of acrylonitrile production refining process |
| CN105084505A (en) * | 2014-05-14 | 2015-11-25 | 中国石油化工股份有限公司 | Method for multi-phase wet-type oxidation processing for industrial waste water |
| CN105600909A (en) * | 2014-11-20 | 2016-05-25 | 中国石油化工股份有限公司 | Catalytic wet oxidation treatment method for organic waste water |
| CN105597740A (en) * | 2014-11-20 | 2016-05-25 | 中国石油化工股份有限公司 | Heterogeneous catalysis wet oxidation catalyst and preparation method thereof |
-
2016
- 2016-10-09 CN CN201610880370.8A patent/CN107915308A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59115786A (en) * | 1982-12-21 | 1984-07-04 | Osaka Gas Co Ltd | Wet oxidation treatment of waste water |
| US20040104181A1 (en) * | 2000-01-05 | 2004-06-03 | Yusuke Shiota | Catalyst for treating waste water, method for preparing the same and process for treating waste water |
| CN103420473A (en) * | 2012-05-16 | 2013-12-04 | 中国石油化工股份有限公司 | Processing method of wastewater of acrylonitrile production refining process |
| CN105084505A (en) * | 2014-05-14 | 2015-11-25 | 中国石油化工股份有限公司 | Method for multi-phase wet-type oxidation processing for industrial waste water |
| CN105600909A (en) * | 2014-11-20 | 2016-05-25 | 中国石油化工股份有限公司 | Catalytic wet oxidation treatment method for organic waste water |
| CN105597740A (en) * | 2014-11-20 | 2016-05-25 | 中国石油化工股份有限公司 | Heterogeneous catalysis wet oxidation catalyst and preparation method thereof |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112441678A (en) * | 2019-09-03 | 2021-03-05 | 中国石油化工股份有限公司 | Method for treating saccharin production wastewater |
| CN112619665A (en) * | 2019-09-24 | 2021-04-09 | 中国石油化工股份有限公司 | Wet oxidation heterogeneous catalyst and preparation method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109574189A (en) | Processing method containing ammonia nitrogen and COD waste water | |
| CN104138756A (en) | Supported catalyzer for low-temperature catalytic combustion of VOCs and method for preparing supported catalyzer for low-temperature catalytic combustion of VOCs | |
| CN111215060A (en) | Preparation of supported platinum group metal monatomic catalyst and application thereof in deoxidation reaction | |
| CN106540694A (en) | Copper-based MOF materials prepare the Cu of porous carbon load2The method of O/Cu composites and its application | |
| Shi et al. | High Performance and Active Sites of a Ceria‐Supported Palladium Catalyst for Solvent‐Free Chemoselective Hydrogenation of Nitroarenes | |
| CN109718806A (en) | A kind of monatomic catalyst of noble metal and its preparation method and application | |
| CN108069500A (en) | A kind of method of ozone catalytic wet oxidation processing organic wastewater | |
| CN101875016A (en) | Catalyst for preparing methane by low-temperature oxidization of methane and preparation method and application thereof | |
| CN111135823B (en) | Wet oxidation catalyst and preparation method and application thereof | |
| CN110327929B (en) | Cobalt-aluminum hydrotalcite derived composite oxide and preparation method and application thereof | |
| CN105916803A (en) | A method for storage and release of hydrogen | |
| CN102108444B (en) | Method for recycling ruthenium in supported type ruthenium catalyst | |
| CN108069501A (en) | A kind of technique for handling organic wastewater | |
| CN104628118B (en) | Catalytic Wet Air Oxidation for Wastewater processing method | |
| CN102101053A (en) | Catalyst for treating organic wastewater and preparation method thereof | |
| CN107915308A (en) | The wet oxidation processing method of high concentrated organic wastewater | |
| CN107913703A (en) | Wet oxidation heterogeneous catalyst | |
| CN105170145A (en) | Catalyst for anoxic dehydrogenation of methanol, and application thereof | |
| JP2009197321A (en) | Noble metal recovering method and noble metal recovering system | |
| CN104399460A (en) | Catalyst for industrial wastewater treatment and preparation method of catalyst | |
| CN107199033A (en) | A kind of preparation method of phenol gas phase hydrogenation preparing cyclohexanone catalyst | |
| CN110433800B (en) | Preparation and application of supported ruthenium catalyst with crystal face effect | |
| CN109569596A (en) | For containing ammonia nitrogen and COD wastewater treatment catalyst | |
| CN106040246A (en) | Nickel-based catalyst and preparation method and application thereof in catalyzing selective hydrogenation of 1,4-butynediol to synthesize 1,4-butylene glycol | |
| Lu et al. | Mechanism in chlorine‐enhanced Pd catalyst for H2O2 in situ synthesis in electro‐Fenton system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180417 |