CN102218337A - Oil and gas field wastewater treatment catalyst and oil and gas field wastewater treatment method - Google Patents
Oil and gas field wastewater treatment catalyst and oil and gas field wastewater treatment method Download PDFInfo
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- CN102218337A CN102218337A CN 201010148428 CN201010148428A CN102218337A CN 102218337 A CN102218337 A CN 102218337A CN 201010148428 CN201010148428 CN 201010148428 CN 201010148428 A CN201010148428 A CN 201010148428A CN 102218337 A CN102218337 A CN 102218337A
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Abstract
The invention relates to an oil and gas field wastewater treatment catalyst and an oil and gas field wastewater treatment method, belongs to the field of oil and gas field wastewater treatment, and particularly relates to a technology for removing chloride ions from the oil and gas field wastewater. A silicate mineral is used as the carrier for the oil and gas field wastewater treatment catalyst, and at least one of silver and palladium is used as the active component, wherein noble metal accounts for 0.02 to 0.07 percent of the total mass of the catalyst. By adopting the catalyst to treat the oil and gas field wastewater, the concentration of chloride ions in the oil and gas field wastewater which contains 20000 to 80000 mg/L of chloride ions and more than 10000 mg/L of COD (Chemical Oxygen Demand) can be reduced to 500 to 1000 mg/L, the concentration of COD can be reduced to 2000 mg/L, the treatment effect is obvious, the treatment cost is low, and no secondary pollution is caused.
Description
Technical field
The present invention relates to a kind of catalyst and oil gas field waste method for treating water of oil gas field waste water treatment, belong to the oil gas field waste water treatment field, relate to especially that chlorion removes technology in the oil gas field waste water.
Background technology
The waste water that oil-gas field development produces mainly is waste water and the probing waste water that produces in the oil-gas mining, mainly contain environmental contaminants such as petroleum-type, organic matter, heavy metal, soda acid thing, chlorion in this class waste water, if in linely will cause very big pollution to the wellblock periphery.At present, be primarily aimed at petroleum-type, organic matter, heavy metal, soda acid thing, do not have suitable method for the chlorion of high concentration always and handle for the improvement of oil gas field waste water.The technology of handling chlorion in the seawater can be used for the oil gas field waste water treatment, as technology such as electrodialysis, film separation, ion-exchanges, but these technology are all inapplicable for the processing of oil gas water in field, except that the hc effluent that also remains nearly 1/3rd after separating can't further be handled, high disposal cost also can't be used these technology.After the most of oil gas field waste water in the whole world all adopt simple process to remove pollutants such as petroleum-type, organic matter, heavy metal, soda acid thing at present,, enter the lake, great river at last by clear water dilution waste water chlorion.
Summary of the invention
The purpose of this invention is to provide chlorion processing method in catalyst that chlorion in a kind of suitable oil gas field waste water handles and the oil gas field waste water.This method treatment effect is obvious, and processing cost is cheap, can not produce secondary pollution.
The catalyst that chlorion is handled in the oil gas field waste water provided by the invention is to be carrier with the silicate mineral, is active component with at least a in silver, the palladium.Wherein, noble metal accounts for the 0.02-0.07% (preferred 0.03-0.05%) of catalyst gross mass.
The preferred palladium of described noble metal.
Preparation of catalysts method provided by the invention be by following steps finish into:
(1) just precious metal salt is ground to granularity 80～100 orders with silicate mineral; Wherein, noble metal accounts for 0.02～0.07% (preferred 0.03-0.05%) of catalyst gross mass; Described precious metal salt is at least a in silver salt, the palladium salt;
(2) granulation: add suitable quantity of water, granulation, particle diameter is 3～5mm;
(3) 8～12 times of calcining promptly in 800～1200 ℃ (preferred 800-1000 ℃) for the catalyst precursor after the granulation.
Adopt catalyst of the present invention, the method for handling oil gas field wastewater may further comprise the steps:
A, oil gas field waste water pretreatment: remove by filter the solid impurity in the oil gas field waste water, finish water-oil separating by oil interceptor;
Add above-mentioned catalyst in the waste water after b, the separation;
C, acid adjustment degree pH=2～4 add ferrous sulfate or aluminum sulfate then, and stirring and dissolving is neutralized to pH=4～6 with limewash, leave standstill 1-2 hour; The addition of ferrous sulfate or aluminum sulfate is to make that ferrous sulfate or aluminum sulfate concentration are 3～7% (percentage by weights) of sewage quantity.
D, separation: adopt Separation of Solid and Liquid, remove solid phase after, chlorion reaches discharge standard in the discharge water, directly discharges.
For the higher waste water of COD, be preferably in add catalyst after, add the oxidant oxidation earlier, with COD in the oil gas water in field reduce to below the 2000mg/L after carry out the c step.
Further preferably c step acid adjustment degree pH=2～4 backs add 3～5% ferrous sulfate earlier, stirring and dissolving, be neutralized to pH=4～6 with limewash, leave standstill filtration in 1～2 hour, add 3～4% aluminum sulfate solutions then again, stirring and dissolving is neutralized to pH=4～6 with limewash, leaves standstill after 1～2 hour to carry out the d step.
The addition of above-mentioned aluminum sulfate or ferrous sulfate determines according to chlorine ion concentration in the oil gas field waste water so that chlorion as far as possible polymerization reaction take place be as the criterion.Usually adopt the multistep treatment system for high-concentration chlorine ion wastewater, every grade of treatment system comprises above-mentioned b, c, d step.Every grade of water inflow next stage treatment system that treatment system is discharged can directly be discharged when chlorion reaches discharge standard in discharge water.
After the d step Separation of Solid and Liquid, the pulpous state solid phase adopts screen cloth to reclaim catalyst granules, recycles; Slurry polymerization iron chloride, aluminium polychloride precipitation send destructor plant to handle after adopting chamber filter press to be pressed into dried cake.
PH is very crucial in the course of reaction, and pH=2～4 when adding ferrous sulfate (or aluminum sulfate) are neutralized to pH=4～6 with limewash, and pH is too high or too low, all influences the muriatic formation of polymerization.
D, separation: adopt Separation of Solid and Liquid, remove solid phase, the COD in the waste water can discharge after advanced treating reaches discharge standard.
The inventive method can be handled chlorine ion concentration 20000～80000mg/L, the oil gas field waste water of COD 2000～10000mg/L, chlorine ion concentration is reduced to 500～1000mg/L in the discharge water, advanced treating was up to standard after COD reduced to 2000mg/L, be suitable for the usefulness of agricultural irrigation, treatment effect is obvious, and processing cost is cheap, can not produce secondary pollution.
The present invention adopts ferrous sulfate or aluminum sulfate can form the polymerization chloride, but for the oil gas water in field, must adopt ferrous sulfate method earlier, adopts the aluminum sulfate method then.Adopt ferrous sulfate method can remove part COD in the oil gas water in field simultaneously, and aluminum sulfate method processing cost is low.
Owing to contain a large amount of sulfate radicals in the water, its chemical potential is lower than chlorion, reaction is active than chlorion, adopt the catalyst of the special development of the present invention, reduce the chlorion chemical potential, make that chlorion is preferential to be generated polymer (poly-ferric chloride, aluminium polychloride) with iron, aluminium ion and precipitate and separate out, removed the chlorion in the waste water.Poly-ferric chloride, aluminum precipitation thing (poly-ferric chloride, aluminium polychloride) are one nontoxic industrial waste.The inventive method is simple, and processing cost is cheap, can satisfy the processing of chlorion in the oil gas field waste water.
Description of drawings
Fig. 1 is a process chart of the present invention.
Fig. 2 is the plane schematic top plan view for the treatment of apparatus of the present invention.
1 is that water pump, 2 is that pretreatment pool, 3 is that current potential counteracting tank, 4 oxidation tanks, 5 are Cl among the figure
-Polymerization tank, 6 is Cl
-The condensate knockout drum, 7 is neutralization pond, 8 is that sand filter, 9 is filter press.
A is that pH conditioning agent (10% sulfuric acid), b are that oxidant (hydrogen peroxide), c are saturated limewater.
The specific embodiment
High-chloride wastewater of the present invention is handled the processing of mud in the processing that is divided into chlorion in the waste water and the technology.
The present invention is further described below in conjunction with drawings and Examples, is limitation of the present invention but should not be construed as, and allly considers carefully modification, replacement, the change made based on above-mentioned technology and all should belong to the present invention.
Just the 5g silver nitrate is ground to granularity 80～100 orders with silicate mineral 10kg; Granulation obtains catalyst precursor, and the catalyst precursor after the granulation promptly got the 10kg catalyst in 9 hours in 1000 ℃ of calcinings.
Just the 5g silver chlorate is ground to granularity 80～100 orders with silicate mineral 10kg; Granulation: obtain catalyst precursor, the catalyst precursor after the granulation promptly got the 10kg catalyst in 9 hours in 1200 ℃ of calcinings.
The 5g palladium bichloride is ground to granularity 80～100 orders with silicate mineral 10kg; Granulation: obtain catalyst precursor, the catalyst precursor after the granulation promptly got the 10kg catalyst in 9 hours in 800 ℃ of calcinings.
Adopt the above-mentioned catalyst can be with about chlorine ion concentration 60000mg/L, chlorine ion concentration is reduced to 500～1000mg/L in the oil gas field waste water about COD7000mg/L, and COD reduces to 2000mg/L, and treatment effect is obvious, processing cost is cheap, can not produce secondary pollution.
Among Fig. 1 and Fig. 2, technology of the present invention is promoted to the preliminary treatment of carrying out waste water in the pretreatment pool 2 by high-chloride wastewater by water pump 1, removes solid impurity at first after filtration, and finishes water-oil separating by oil interceptor.Enter Cl after the processing
-The position district falls, Cl
-Under certain conditions and under catalyst action of the present invention, chemical potential descends, and enters Cl
-Polymeric area exists and Cl in polymeric area
-The condensate of polymerization carries out polymerisation and forms polymer.Separation of Solid and Liquid, mud by collect, concentrate, press filtration becomes the dewatered sludge outward transport to handle or use as simple water treatment agent.The present invention is added with in technology and is beneficial to catalysis, adjusting, the nertralizer that produces various environmental conditions, enter catalysis-poly-iron processing unit through pretreated waste water, filter after generating poly-ferric chloride, filter liquor enters next poly-aluminium processing unit, the aluminium polychloride that generates also removes by filter, measure the concentration of chlorion in the filter liquor, according to the progression of the concentration decision treatment system of chlorion in the filter liquor, until the qualified discharge standard.
It below is the instantiation that adopts catalyst of the present invention that oil gas field waste water is handled.
By water pump 1, preliminary treatment 2, Cl
-The Cl of current potential counteracting tank 3, preparation
-Current potential is subdued agent 4, Cl
-Polymerization tank 5, Cl
-Condensate knockout drum 6 compositions also are connected to form a Cl
-Processing unit.
For meeting the demands, cell cube end of the present invention can be set up one-level SS treating apparatus (filter).
At whole C l
-Being divided into 4 indispensable treatment regions in the processing procedure is pretreating zone, Cl
-Position district, Cl fall
-Polymeric area and Disengagement zone constitute, and form a high Cl
-The cell cube that concentration is handled, in practice, can be according to high Cl
-The height of concentration and the standard of emission request will be combined into single or multiple cell cubes, constitute a perfect high chlorine sewage disposal system.
Test example 1 adopts catalyst of the present invention that oil gas field waste water is handled
A, oil gas field waste water pretreatment: the about 60000mg/L of chlorine ion concentration, the oil gas field waste water of COD7000mg/L, solids removed by filtration impurity is finished water-oil separating by oil interceptor;
Waste water after b, the separating oil adds 3% hydrogen peroxide (30% mass percent concentration) oxidation;
Waste water after c, the hydrogen peroxide treatment adds in the catalyst 100kg/t water pot that embodiment 1 preparation is housed.
15～20 ℃ of room temperatures, acid adjustment degree are pH=2, add ferrous sulfate and are stirred to dissolving, are neutralized to pH=4～6 with limewash then, leave standstill 1.5 hours; Ferrous sulfate concentration is 6%;
D, separation: adopt Separation of Solid and Liquid, reclaim catalyst, remove poly-ferric chloride, aluminium polychloride precipitation, chlorine ion concentration is reduced to 800mg/L in the water of discharge, and COD reduces to 500mg/L, is suitable for the usefulness of agricultural irrigation.
Test example 2 adopts catalyst of the present invention that oil gas field waste water is handled
A, oil gas field waste water pretreatment: the about 60000mg/L of chlorine ion concentration, the oil gas field waste water of COD7000mg/L, solids removed by filtration impurity is finished water-oil separating by oil interceptor;
Waste water after b, the separating oil adds 2% hydrogen peroxide (30% concentration) oxidation;
Waste water after c, the hydrogen peroxide treatment adds in the catalyst 80kg/t water pot that embodiment 2 preparations are housed.
15～20 ℃ of room temperatures, acid adjustment degree are pH=3, add ferrous sulfate and are stirred to dissolving, are neutralized to pH=6 with limewash then, leave standstill 1 hour; Copperas solution concentration is 4%;
D, add aluminum sulfate then, stirring and dissolving is neutralized to pH=5 with limewash then, leaves standstill 2 hours; Aluminum sulfate solution concentration is 3%;
E, separation: adopt Separation of Solid and Liquid, reclaim catalyst, remove poly-ferric chloride, aluminium polychloride precipitation, chlorine ion concentration is reduced to 700mg/L in the water of discharge, and COD reduces to 500mg/L, is suitable for the usefulness of agricultural irrigation.
Test example 3 adopts catalyst of the present invention that oil gas field waste water is handled
A, oil gas field waste water pretreatment: the about 60000mg/L of chlorine ion concentration, the oil gas field waste water of COD7000mg/L, solids removed by filtration impurity is finished water-oil separating by oil interceptor;
Waste water after b, the separating oil adds hydrogen peroxide (30% concentration) oxidation of wastewater flow rate 3%;
Waste water after c, the hydrogen peroxide treatment adds in the catalyst 50kg/t water pot that embodiment 3 preparations are housed.
15～20 ℃ of room temperatures, acid adjustment degree are pH=4, add ferrous sulfate and are stirred to dissolving, are neutralized to pH=6 with limewash then, leave standstill 1.5 hours; Copperas solution concentration is 3%;
D, add aluminum sulfate then, stirring and dissolving is neutralized to pH=6 with limewash then, leaves standstill 2 hours; Aluminum sulfate solution concentration is 4%;
E, separation: adopt Separation of Solid and Liquid, reclaim catalyst, remove poly-ferric chloride, aluminium polychloride precipitation, chlorine ion concentration is reduced to 500mg/L in the water of discharge, and COD reduces to 500mg/L, is suitable for the usefulness of agricultural irrigation.
For high-concentration chlorine ion wastewater, adopt the multistep treatment system, every grade of treatment system repeats b, c, d, e step.
Test example 4 adopts catalyst of the present invention that oil gas field waste water is handled
Adopt embodiment 1 identical method to prepare following catalyst, and adopt this catalyst to the about 61590mg/L of chlorine ion concentration, the oil gas field waste water of COD7000mg/L is handled.Handle forward and backward chlorine ion concentration and see Table 1.
| Batch | The loading of active component and active component | The catalyst charge weight | Chlorine ion concentration before handling | Handle the back |
| 1 | Ag/0.05％ | 0 | 61590mg/L | 59000mg/ |
| 2 | Ag/0.05％ | 50kg/t water | 61590mg/L | 48500mg/ |
| 3 | Ag/0.05％ | 100kg/t water | 61590mg/L | 12799mg/ |
| 4 | Ag/0.05％ | 150kg/t water | 61590mg/L | 12590mg/ |
| 5 | Ag/0.05％ | 200kg/t water | 61590mg/L | 12500mg/ |
| 6 | Pd/0.03％ | 0 | 61590mg/L | 58920mg/ |
| 7 | Pd/0.03％ | 30kg/t water | 61590mg/L | 49870mg/ |
| 8 | Pd/0.03％ | 90kg/t water | 61590mg/L | 9800mg/ |
| 9 | Pd/0.03％ | 120kg/t water | 61590mg/L | 9650mg/L |
Table 1 result shows: that treatment effect is best is catalyst P d/0.03%.Factors such as integrated cost consider that the optimum quantum of utilization of catalyst P d/0.03% is a 120kg/t water.
Claims (10)
1. the catalyst that chlorion is handled in the oil gas field waste water, it is characterized in that: it is to be carrier with the silicate mineral, is active component with at least a in silver, the palladium, wherein, noble metal accounts for 0.02～0.07% (preferred 0.03～0.05%) of catalyst gross mass.
2. according to the catalyst of chlorion processing in the described oil gas field waste water of claim 1, it is characterized in that: described noble metal is a palladium.
3. the Preparation of catalysts method that chlorion is handled in the oil gas field waste water, it is characterized in that be by following steps finish into:
(1) just precious metal salt is ground to granularity 80～100 orders with silicate mineral; Wherein, noble metal accounts for 0.02～0.07% of catalyst gross mass; Described precious metal salt is at least a in silver salt, the palladium salt;
(2) granulation: add suitable quantity of water, granulation obtains catalyst precursor, and particle diameter is 3～5mm;
(3) catalyst precursor calcined for 8～12 times promptly in 800～1200 ℃.
4. the Preparation of catalysts method that chlorion is handled in the oil gas field waste water according to claim 3 is characterized in that: 800～1000 ℃ of catalyst precursor calcining heats.
5. the method for handling oil gas field wastewater is characterized in that may further comprise the steps:
A, oil gas field waste water pretreatment: remove by filter the solid impurity in the oil gas field waste water, finish water-oil separating by oil interceptor;
Add each described catalyst of claim 1-3 in the waste water after b, the separation;
C, acid adjustment degree pH=2～4 add ferrous sulfate or aluminum sulfate then, and stirring and dissolving is neutralized to pH=4～6 with limewash, leave standstill 1-2 hour; Wherein, after adding ferrous sulfate or the aluminum sulfate stirring and dissolving, the concentration of ferrous sulfate or aluminum sulfate is 3～7%;
D, separation: adopt Separation of Solid and Liquid, remove that the COD in the waste water can discharge after the solid phase after advanced treating.
6. the method for handling oil gas field wastewater according to claim 5 is characterized in that: the b step adds the oxidant oxidation after adding catalyst, with COD in the oil gas water in field reduce to below the 2000mg/L after carry out the c step.
7. the method for handling oil gas field wastewater according to claim 6, it is characterized in that: c step acid adjustment degree pH=2～4 backs add ferrous sulfate earlier, stirring and dissolving, be neutralized to pH=4～6, leave standstill filtration in 1-2 hour, add aluminum sulfate again, stirring and dissolving after then, be neutralized to pH=4～6, leave standstill after 1～2 hour and carry out the d step;
Wherein the addition of ferrous sulfate or aluminum sulfate reaches 3～7% for the ferrous sulfate that makes or the concentration of aluminum sulfate.
8. according to the method for each described handling oil gas field wastewater of claim 5～7, it is characterized in that: after the d step Separation of Solid and Liquid, reclaim catalyst granules and recycle.
9. according to the method for each described handling oil gas field wastewater of claim 5～7, it is characterized in that: chlorine ion concentration 20000～80000mg/L in the oil gas field waste water, COD 2000～10000mg/L.
10. according to the method for each described handling oil gas field wastewater of claim 5～7, it is characterized in that: for high-concentration chlorine ion wastewater, adopt the multistep treatment system, every grade of treatment system repeats b, c, d step.
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| CN102218337B CN102218337B (en) | 2013-02-06 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105293774A (en) * | 2015-11-18 | 2016-02-03 | 金川集团股份有限公司 | Method for increasing recovery rate of precious metals in waste liquid |
| CN106630253A (en) * | 2016-10-20 | 2017-05-10 | 中北大学 | Coking wastewater chloride ion removing pretreatment method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86104833A (en) * | 1986-07-11 | 1987-04-22 | 张鸿儒 | The production method of Method of high accumulative aluminium-ferric flocculant |
| WO1994003394A1 (en) * | 1992-08-04 | 1994-02-17 | Bayer Aktiengesellschaft | Removal of chlorine from hydrogen gas mixtures by conversion in the presence of platinum or palladium catalysts |
| CN1096498A (en) * | 1992-09-06 | 1994-12-21 | 德国索尔瓦有限公司 | From wastewater treatment method and equipment the Epicholorohydrin biology, that contain organism, especially organochlorine compound |
| CN1130882A (en) * | 1994-03-01 | 1996-09-11 | 德国索尔瓦有限公司 | Process for catalytically treating waste water and process for regenerating catalyst |
-
2010
- 2010-04-16 CN CN 201010148428 patent/CN102218337B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86104833A (en) * | 1986-07-11 | 1987-04-22 | 张鸿儒 | The production method of Method of high accumulative aluminium-ferric flocculant |
| WO1994003394A1 (en) * | 1992-08-04 | 1994-02-17 | Bayer Aktiengesellschaft | Removal of chlorine from hydrogen gas mixtures by conversion in the presence of platinum or palladium catalysts |
| CN1096498A (en) * | 1992-09-06 | 1994-12-21 | 德国索尔瓦有限公司 | From wastewater treatment method and equipment the Epicholorohydrin biology, that contain organism, especially organochlorine compound |
| CN1130882A (en) * | 1994-03-01 | 1996-09-11 | 德国索尔瓦有限公司 | Process for catalytically treating waste water and process for regenerating catalyst |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105293774A (en) * | 2015-11-18 | 2016-02-03 | 金川集团股份有限公司 | Method for increasing recovery rate of precious metals in waste liquid |
| CN106630253A (en) * | 2016-10-20 | 2017-05-10 | 中北大学 | Coking wastewater chloride ion removing pretreatment method |
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