CN102442745A - Treatment method of high-concentration waste water during methanol-to-olefin process - Google Patents
Treatment method of high-concentration waste water during methanol-to-olefin process Download PDFInfo
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Abstract
The invention relates to a treatment method of high-concentration waste water during methanol-to-olefins (MTO) process, wherein after MTO high-concentration process waste water is treated by the treatment flow of homogeneous regulation, oil-removing coagulating sedimentation, high-efficient anaerobic treatment and post-precipitation, and corresponding condition, the COD of the waste water is reduced to be less than 2000 mg/L from about 50000 mg/L, and the removal rate is more than 96%. The treatment method of high-concentration waste water during methanol-to-olefin process has stable treatment effect, simple and convenient operation and low treatment cost, is easy to commercially produce and can be used for pre-treating MTO high-concentration process waste water before entering the normal sewage treatment plant to be treated aerobically and biologically.
Description
Technical field
The present invention relates to the treatment process of organic chemical waste water in the technical field of waste water processing, is a kind of high concentration methanol system olefin process wastewater treatment method specifically.
Background technology
Along with development and national economy, soaring day by day to low-carbon alkene demands such as basic Organic Chemicals ethene, propylene especially is as the situation of resources face worsening shortages such as the petroleum naphtha of low-carbon alkene traditional raw material, solar oil.Therefore accelerate the extensive attention that the relevant application that substitutes production technology has caused social each side.
In recent years, by coal or natural gas via methanol-to-olefins (MTO) technology in the world technological development reach its maturity, have significantly competition potential.Under the higher form of at present crude oil worsening shortages and price, the MTO technology is expected to step in a short time the industrial applications stage.
The reaction mechanism of MTO is that methanol dehydration generates dme, and the equilibrium mixture of dme and methyl alcohol dewaters then, and to change into ethene, propylene be master's low-carbon alkene and a small amount of stable hydrocarbon and aromatic hydrocarbons etc.Generate a large amount of water because dehydration reaction is inevitable in the reaction process; These water and unreacted methanol and some intermediate products leave reactor drum with the form of gas with product; Be referred to as reaction gas, after reaction gas entering quench tower cooled off, liquefaction such as water vapor and methyl alcohol was liquid; At the bottom of the chilling Tata, discharge together, form one high density spent process water.This strand waste water water yield is less relatively, but contains a large amount of oxygen-bearing organic matters that from mixed gas, wash out in the waste water, and pollutant load is high.If this strand waste water is not carried out pre-treatment, and directly being disposed to conventional sewage-farm, it handles, then can not satisfy the influent quality requirement in sewage-farm, can not guarantee the normal and stable running in sewage-farm and the requirement up to standard of externally discharged waste water.
Chinese patent CN 101353187 provides a kind of MTO prewhirl flow type reaction waste vapor stripping purifying method, and this method comprises: the MTO reaction waste is carried out little rotational flow separation, to remove the granules of catalyst that wherein contains.A kind of MTO prewhirl flow type reaction waste vapor stripping refining plant also is provided.But this patent has only proposed the method for separating catalyst particles from the MTO reaction waste, and the not mentioned waste water of how handling.
A kind of waste water treatment process that contains methyl alcohol and dme is disclosed among the Chinese patent CN101139118A; Its concrete grammar is: the waste water that will contain methyl alcohol and dme; The pressurization back and the heat exchange of purifying waste water at the bottom of the stripping Tata; Get into stripping tower then, the gaseous mixture such as methyl alcohol that the stripping tower cat head produces get into return tank after heat exchange, and a part is returned the stripping tower cat head as backflow; It is outer or as the raw material of MTO device that another part is delivered to device; Go out to purify waste water at the bottom of the stripping Tata, and deliver to outside the device after the wastewater heat exchange that contains methyl alcohol and dme.Point out in the patent that after this art breading, the total content of methyl alcohol and dme can reach below the 100ppm during gained was purified waste water.As for whether also containing other pollution substance in purifying waste water and how further handling purifying waste water, this patent is also not mentioned.
Can find out from above disclosed document; MTO wastewater treatment means mainly concentrate on the physical sepn of water and pollutent at present; And the method for wastewater treatment that is proposed also only is principle, how further deeply to handle as for the waste water of the needs discharging especially waste water of high density and then do not mention basically.
Summary of the invention
To the defective that exists in the prior art, the object of the present invention is to provide a kind of high concentration methanol system olefin process wastewater treatment method, can significantly cut down MTO and produce the total amount of pollutant, to remedy the deficiency of prior art to environmental emission.
For reaching above purpose, the technical scheme that the present invention takes is:
A kind of high concentration methanol system olefin process wastewater treatment method is characterized in that its concrete steps are:
In the 1st step, adopt the homogeneous regulating measure to handle to high density MTO spent process water: wastewater pH is adjusted to 6～8, and the pH regulator agent of employing is a sodium hydroxide solution, and waste water is 6～48h at the mean residence time of homogeneous regulon;
In the 2nd step, the oil removal coagulating sedimentation is handled: in the high density MTO spent process water of regulating through homogeneous, add coagulating agent, carry out the oil removal coagulating sedimentation; Coagulating agent adopts Poly aluminum Chloride (PAC), and the consumption of Poly aluminum Chloride (PAC) is 20～150mg/L;
In the 3rd step, efficient anaerobic is handled: the device that efficient anaerobic is handled adopts the internal recycle high efficiency anaerobic reactor, adopts anaerobic grain sludge to inoculate and handles waste water; The main control parameters that efficient anaerobic is handled is following:
(1) sludge concentration is 10～50g/L;
(2) the COD volumetric loading is 5～50kg/ (m
3D);
(3) the anaerobic reaction temperature is controlled at 20～40 ℃;
(4) when carrying out anaerobic treatment, need in waste water, to add N nutritive salt and P nutritive salt, the ratio of adding is COD: N: P=300～500: 5: 1;
In the 4th step, settling tank is set carries out the postprecipitation processing: the ST is 1.5～4.5h; The hydraulic surface loading of final settling tanks is 0.45～0.80m
3/ (m
2The anaerobic sludge of h), discharging from final settling tanks is further handled by the conventional processing measure as excess sludge.
On the basis of technique scheme; In the 1st step, when adopting the homogeneous regulating measure to handle, wastewater pH is adjusted to 6.5～7.5 to high density MTO spent process water; The pH regulator agent of adopting is a sodium hydroxide solution, and waste water is 12～24h at the mean residence time of homogeneous regulon.
On the basis of technique scheme, in the 2nd step, when the oil removal coagulating sedimentation was handled, the consumption of Poly aluminum Chloride (PAC) was 50～120mg/L.
On the basis of technique scheme, when the oil removal coagulating sedimentation is handled, also add SEPIGEL 305, the consumption of SEPIGEL 305 is 0～10mg/L.
On the basis of technique scheme, the consumption of SEPIGEL 305 is 0～5mg/L.
On the basis of technique scheme, during efficient anaerobic was handled, the N nutritive salt that adds was urea or ammonium chloride, and the P nutritive salt that adds is tsp or potassium primary phosphate.
On the basis of technique scheme, during efficient anaerobic was handled, outer circulation was carried out in the water outlet of internal recycle high efficiency anaerobic reactor, and recycle ratio is 0～50: 1.
On the basis of technique scheme, when efficient anaerobic is handled, in the internal recycle high efficiency anaerobic reactor, to inoculate and handle waste water with anaerobic grain sludge, the main control parameters that efficient anaerobic is handled is following:
(1) sludge concentration is 15～30g/L;
(2) the COD volumetric loading is 15～35kg/ (m
3D);
(3) reactor drum water outlet recycle ratio is 5: 1～10: 1;
(4) the anaerobic reaction temperature is 25～35 ℃;
(5) ratio of adding of N nutritive salt and P nutritive salt is COD: N: P=350～500: 5: 1.
On the basis of technique scheme, settling tank is set carries out postprecipitation when handling, the ST is 2～4h; The hydraulic surface loading of final settling tanks is 0.50～0.75m
3/ (m
2H).
High concentration methanol system olefin process wastewater treatment method of the present invention; Treatment effect is stable, easy and simple to handle, processing cost is low; Be easy to realize industrial application; Can be used for high density MTO spent process water and get into conventional sewage-farm aerobic biochemical processing pre-treatment before; That is: can be used as high density MTO spent process water and get into the preprocessing means before the conventional sewage-farm, guarantee that high density MTO spent process water organic pollutant content after this pre-treatment reduces greatly, get into conventional sewage-farm again and handle and be easy to reach emission standard.
Description of drawings
The present invention has following accompanying drawing:
Fig. 1 process flow diagram of the present invention.
Embodiment
Below in conjunction with accompanying drawing the present invention is done further explain.
High density MTO spent process water mainly comes from draining at the bottom of the MTO reaction mixture gas body chilling Tata, contains a large amount of oxygen-bearing organic matters that from mixed gas, wash out, and organic pollutant content is high.Its main water quality situation is following:
1, water temperature is 25～45 ℃;
2, pH is 3～5;
3, COD is 40000～60000mg/L; Wherein methanol content is 8000～12000mg/L, and acetic acid content is 3000～6000mg/L, and acetone content is 6000～9000mg/L; Petroleum content is 800～2000mg/L, contains organic pollutants such as formaldehyde, acetaldehyde, ethanol, methylethylketone in addition;
4, SS is 1000～10000mg/L;
5, specific conductivity is 2000～5000 μ S/cm.
According to the water quality characteristics of high density MTO spent process water COD height, good biodegradability, the present invention proposes the processing technological flow of homogeneous adjusting-oil removal coagulating sedimentation-efficient anaerobic-postprecipitation, and each flow process has all been provided corresponding technological conditions.Processing technological flow figure sees Fig. 1, and its concrete steps are:
In the 1st step, adopt the homogeneous regulating measure to handle to high density MTO spent process water: wastewater pH to be adjusted to 6～8, for example: can be with pH regulator to 6,6.5,7,7.5 or 8; The pH regulator agent of adopting is a sodium hydroxide solution, and waste water is 6～48h at the mean residence time of homogeneous regulon; For example: mean residence time is between 6～48h, and every increase 0.5h both can be used as a specific embodiment;
For fluctuation and the waste water that reduces manufacturing condition is the disadvantageous effect that tart character is brought wastewater treatment; The present invention at first adopts conventional homogeneous regulating measure to handle to high density MTO spent process water, and purpose is the water yield and the water conditioning that as far as possible guarantees subsequent processes;
After adjusting was handled through homogeneous, the main water quality situation of water outlet is following: water temperature was 25～40 ℃, and pH is 6.5～7.5; COD is 45000～58000mg/L, and methanol content is 9000～11000mg/L, and acetic acid content is 4000～5000mg/L; Acetone content is 6500～8000mg/L; Petroleum content is 800～1500mg/L, and SS is 2000～8000mg/L, and specific conductivity is 3000～6000 μ S/cm;
In the 2nd step, the oil removal coagulating sedimentation is handled: in the high density MTO spent process water of regulating through homogeneous, add coagulating agent, carry out the oil removal coagulating sedimentation; Coagulating agent adopts Poly aluminum Chloride (PAC), and the consumption of Poly aluminum Chloride (PAC) is 20～150mg/L; For example: the consumption of Poly aluminum Chloride (PAC) is between 20～150mg/L, and every increase 5mg/L both can be used as a specific embodiment;
After high density MTO spent process water being carried out homogeneous adjusting processing, next to carry out the oil removal coagulating sedimentation and handle, purpose is oil slick and the suspended substance of removing in the water;
After the processing of oil removal coagulating sedimentation, waste water PetroChina Company Limited. class content can be reduced to below the 50mg/L, and SS can be reduced to below the 100mg/L.Oil slick and waste residue that the oil removal precipitation process of coagulation produces then can further be handled by the conventional processing measure;
In the 3rd step, efficient anaerobic is handled: the device that efficient anaerobic is handled adopts internal recycle high efficiency anaerobic reactor (being the IC reactor drum), adopts anaerobic grain sludge to inoculate and handles waste water;
In order to ensure the steady running of system for anaerobic treatment, the main control parameters that efficient anaerobic is handled is following:
(1) sludge concentration is 10～50g/L; For example: can be 10g/L, 15g/L, 20g/L, 25g/L, 30g/L, 35g/L, 40g/L, 45g/L or 50g/L;
(2) the COD volumetric loading is 5～50kg/ (m
3D); For example: can be 5kg/ (m
3D), 10kg/ (m
3D), 15kg/ (m
3D), 20kg/ (m
3D), 25kg/ (m
3D), 30kg/ (m
3D), 35kg/ (m
3D), 40kg/ (m
3D), 45kg/ (m
3D) or 50kg/ (m
3D);
(3) the anaerobic reaction temperature is controlled at 20～40 ℃; For example: can be 20 ℃, 25 ℃, 30 ℃, 35 ℃ or 40 ℃;
(4) owing to lack N and P in the MTO spent process water, so when carrying out anaerobic treatment, need in waste water, add N nutritive salt and P nutritive salt, the ratio of adding is COD: N: P=300～500: 5: 1; For example: the ratio of adding can be 300: 5: 1,350: 5: 1,400: 5: 1,450: 5: 1 or 500: 5: 1;
High density MTO spent process water is after homogeneous is regulated processing and the processing of oil removal coagulating sedimentation; Next carrying out efficient anaerobic handles; Because the contained organic pollutant overwhelming majority all is the material of readily biodegradable in the MTO spent process water, can obtain than higher COD clearance so adopt efficient anaerobic to handle;
In the 4th step, settling tank is set carries out the postprecipitation processing: the ST is 1.5～4.5h; The hydraulic surface loading of final settling tanks is 0.45～0.80m
3/ (m
2The anaerobic sludge of h), discharging from final settling tanks is further handled by the conventional processing measure as excess sludge; For example: the ST can be 1.5h, 2h, 2.5h, 3h, 3.5h, 4h or 4.5h; The hydraulic surface loading of final settling tanks can be 0.45m
3/ (m
2H), 0.50m
3/ (m
2H), 0.55m
3/ (m
2H), 0.60m
3/ (m
2H), 0.65m
3/ (m
2H), 0.70m
3/ (m
2H), 0.75m
3/ (m
2H) or 0.80m
3/ (m
2H);
After anaerobic treatment, be entrained with some anaerobic sludges in the water outlet, SS is 150～800mg/L, therefore causes water outlet COD higher, is 2000～4000mg/L; Be beneficial to subsequent disposal in order to carry out mud-water separation, settling tank be set carry out the postprecipitation processing;
High density MTO spent process water is after above-mentioned flow processing, and waste water COD can be reduced to below the 2000mg/L, and clearance reaches more than 95%; Waste water PetroChina Company Limited. class can be reduced to below the 30mg/L, and SS can be reduced to below the 70mg/L, thereby the organic pollutant content that gets into conventional sewage-farm in the waste water is significantly reduced, and reaches the water inlet requirement that composite wastewater is handled the field fully.
On the basis of technique scheme; When adopting the homogeneous regulating measure to handle to high density MTO spent process water; Wastewater pH is adjusted to 6.5～7.5, and the pH regulator agent of employing is a sodium hydroxide solution, and waste water is 12～24h at the mean residence time of homogeneous regulon.
On the basis of technique scheme, when the oil removal coagulating sedimentation was handled, the consumption of Poly aluminum Chloride (PAC) was 50～120mg/L.
On the basis of technique scheme, when the oil removal coagulating sedimentation is handled, also add SEPIGEL 305, the consumption of SEPIGEL 305 is 0～10mg/L.
On the basis of technique scheme, the consumption of SEPIGEL 305 is 0～5mg/L.
On the basis of technique scheme, during efficient anaerobic was handled, the N nutritive salt that adds was urea or ammonium chloride, and the P nutritive salt that adds is tsp or potassium primary phosphate.
On the basis of technique scheme, during efficient anaerobic was handled, outer circulation was carried out in the water outlet of internal recycle high efficiency anaerobic reactor, and recycle ratio is 0～50: 1.For example: recycle ratio can be 1: 1,10: 1,20: 1,30: 1,40: 1 or 50: 1.
On the basis of technique scheme, when efficient anaerobic is handled, in the internal recycle high efficiency anaerobic reactor, to inoculate and handle waste water with anaerobic grain sludge, the main control parameters that efficient anaerobic is handled is following:
(1) sludge concentration is 15～30g/L;
(2) the COD volumetric loading is 15～35kg/ (m
3D);
(3) reactor drum water outlet recycle ratio is 5: 1～10: 1;
(4) the anaerobic reaction temperature is 25～35 ℃;
(5) ratio of adding of N nutritive salt and P nutritive salt is COD: N: P=350～500: 5: 1.
On the basis of technique scheme, settling tank is set carries out postprecipitation when handling, the ST is 2～4h; The hydraulic surface loading of final settling tanks is 0.50～0.75m
3/ (m
2H).
High concentration methanol system olefin process wastewater treatment method of the present invention; Greatly alleviate high density MTO spent process water and directly got into the pressure that bring in conventional sewage-farm; Waste water through above-mentioned processing is handled through further conventional aerobic biochemical again; Can be easy to reach national wastewater discharge standard, final directly discharging or reuse.
It below is specific embodiment.
Embodiment 1
High density MTO spent process water is the homogenization treatment of 24h at the homogeneous regulon through mean residence time, and regulates pH through adding sodium hydroxide solution, and the main water-quality guideline of water outlet is following: water temperature is 35 ℃; PH is 6.5, and COD is 45500mg/L, and methanol content is 9500mg/L; Acetic acid content is 4050mg/L, and acetone content is 6650mg/L, and petroleum content is 900mg/L; SS is 2300mg/L, and specific conductivity is 3560 μ S/cm.
In oil removal coagulating sedimentation unit, coagulating agent adopts Poly aluminum Chloride (PAC) and SEPIGEL 305, and wherein the Poly aluminum Chloride (PAC) consumption is 50mg/L, and the SEPIGEL 305 consumption is 5mg/L.After the processing of oil removal coagulating sedimentation, waste water PetroChina Company Limited. class drops to 20mg/L, and SS drops to 50mg/L.
At the efficient anaerobic processing unit, add anaerobic grain sludge in the IC reactor drum, sludge concentration is 15g/L, control reaction COD volumetric loading is 15kg/ (m
3D), reactor drum water outlet recycle ratio is 10: 1; Temperature of reaction is controlled at 25 ℃; By COD: N: P=500: add urea and potassium primary phosphate at 5: 1.Under above-mentioned control condition, the COD of anaerobism water outlet can drop to 3850mg/L, and SS is 780mg/L.
In the postprecipitation unit, the control postprecipitation time is 4h, and hydraulic surface loading is 0.80m
3/ (m
2H), the water quality situation of postprecipitation water outlet is following: pH is 8.2, and COD is 1200mg/L, and petroleum-type is 15mg/L, and SS is 50mg/L.Final COD clearance is 97%.
Handle by ordinary method with the waste residue of oil removal coagulating sedimentation unit discharge as excess sludge from the anaerobic sludge that final settling tanks is discharged, be introduced into sludge sump, add the 15mg/L SEPIGEL 305, be delivered to the band filter then and process the filter cake outward transport.
Embodiment 2
High density MTO spent process water is the homogenization treatment of 12h at the homogeneous regulon through mean residence time, and regulates pH through adding sodium hydroxide solution, and the main water-quality guideline of water outlet is following: water temperature is 25 ℃; PH is 7.0, and COD is 50500mg/L, and methanol content is 10100mg/L; Acetic acid content is 4500mg/L, and acetone content is 7200mg/L, and petroleum content is 1050mg/L; SS is 5200mg/L, and specific conductivity is 4560 μ S/cm.
In oil removal coagulating sedimentation unit, coagulating agent adopts Poly aluminum Chloride (PAC) and SEPIGEL 305, and wherein the Poly aluminum Chloride (PAC) consumption is 80mg/L, and the SEPIGEL 305 consumption is 5mg/L.After the processing of oil removal coagulating sedimentation, waste water PetroChina Company Limited. class drops to 35mg/L, and SS drops to 65mg/L.
At the efficient anaerobic processing unit, add anaerobic grain sludge in the IC reactor drum, sludge concentration is 20g/L, control reaction COD volumetric loading is 25kg/ (m
3D), reactor drum water outlet recycle ratio is 5: 1; Temperature of reaction is controlled at 30 ℃; By COD: N: P=500: add urea and potassium primary phosphate at 5: 1.Under above-mentioned control condition, the COD of anaerobism water outlet can drop to 3050mg/L, and SS is 530mg/L.
In the postprecipitation unit, the control postprecipitation time is 2h, and hydraulic surface loading is 0.70m
3/ (m
2H), the water quality situation of postprecipitation water outlet is following: pH is 8.4, and COD is 1500mg/L, and petroleum-type is 10mg/L, and SS is 45mg/L.Final COD clearance is 97%.
Handle by ordinary method with the waste residue of oil removal coagulating sedimentation unit discharge as excess sludge from the anaerobic sludge that final settling tanks is discharged, be introduced into sludge sump, add the 10mg/L SEPIGEL 305, be delivered to the band filter then and process the filter cake outward transport.
Embodiment 3
High density MTO spent process water is the homogenization treatment of 12h at the homogeneous regulon through mean residence time, and regulates pH through adding sodium hydroxide solution, and the main water-quality guideline of water outlet is following: water temperature is 40 ℃; PH is 7.5, and COD is 55500mg/L, and methanol content is 11000mg/L; Acetic acid content is 4950mg/L, and acetone content is 8000mg/L, and petroleum content is 1450mg/L; SS is 7800mg/L, and specific conductivity is 5960 μ S/cm.
In oil removal coagulating sedimentation unit, coagulating agent adopts Poly aluminum Chloride (PAC) and SEPIGEL 305, and wherein the Poly aluminum Chloride (PAC) consumption is 120mg/L, does not add SEPIGEL 305.After the processing of oil removal coagulating sedimentation, waste water PetroChina Company Limited. class drops to 45mg/L, and SS drops to 70mg/L.
At the efficient anaerobic processing unit, add anaerobic grain sludge in the IC reactor drum, sludge concentration is 30g/L, control reaction COD volumetric loading is 35kg/ (m
3D), reactor drum water outlet recycle ratio is 5: 1; Temperature of reaction is controlled at 35 ℃; By COD: N: P=350: add urea and potassium primary phosphate at 5: 1.Under above-mentioned control condition, the COD of anaerobism water outlet can drop to 2350mg/L, and SS is 180mg/L.
In the postprecipitation unit, the control postprecipitation time is 2h, and hydraulic surface loading is 0.50m
3/ (m
2H), the water quality situation of postprecipitation water outlet is following: pH is 8.6, and COD is 1950mg/L, and petroleum-type is 20mg/L, and SS is 60mg/L.Final COD clearance is 96%.
Handle by ordinary method with the waste residue of oil removal coagulating sedimentation unit discharge as excess sludge from the anaerobic sludge that final settling tanks is discharged, be introduced into sludge sump, add the 8mg/L SEPIGEL 305, be delivered to the band filter then and process the filter cake outward transport.
Claims (9)
1. high concentration methanol system olefin process wastewater treatment method is characterized in that its concrete steps are:
In the 1st step, adopt the homogeneous regulating measure to handle to high density MTO spent process water: wastewater pH is adjusted to 6～8, and the pH regulator agent of employing is a sodium hydroxide solution, and waste water is 6～48h at the mean residence time of homogeneous regulon;
In the 2nd step, the oil removal coagulating sedimentation is handled: in the high density MTO spent process water of regulating through homogeneous, add coagulating agent, carry out the oil removal coagulating sedimentation; Coagulating agent adopts Poly aluminum Chloride (PAC), and the consumption of Poly aluminum Chloride (PAC) is 20～150mg/L;
In the 3rd step, efficient anaerobic is handled: the device that efficient anaerobic is handled adopts the internal recycle high efficiency anaerobic reactor, adopts anaerobic grain sludge to inoculate and handles waste water; The main control parameters that efficient anaerobic is handled is following:
(1) sludge concentration is 10～50g/L;
(2) the COD volumetric loading is 5～50kg/ (m
3D);
(3) the anaerobic reaction temperature is controlled at 20～40 ℃;
(4) when carrying out anaerobic treatment, need in waste water, to add N nutritive salt and P nutritive salt, the ratio of adding is COD: N: P=300～500: 5: 1;
In the 4th step, settling tank is set carries out the postprecipitation processing: the ST is 1.5～4.5h; The hydraulic surface loading of final settling tanks is 0.45～0.80m
3/ (m
2The anaerobic sludge of h), discharging from final settling tanks is further handled by the conventional processing measure as excess sludge.
2. high concentration methanol system olefin process wastewater treatment method as claimed in claim 1; It is characterized in that: in the 1st step; When adopting the homogeneous regulating measure to handle to high density MTO spent process water; Wastewater pH is adjusted to 6.5～7.5, and the pH regulator agent of employing is a sodium hydroxide solution, and waste water is 12～24h at the mean residence time of homogeneous regulon.
3. high concentration methanol system olefin process wastewater treatment method as claimed in claim 1 is characterized in that: in the 2nd step, when the oil removal coagulating sedimentation was handled, the consumption of Poly aluminum Chloride (PAC) was 50～120mg/L.
4. high concentration methanol system olefin process wastewater treatment method as claimed in claim 1 is characterized in that: when the oil removal coagulating sedimentation is handled, also add SEPIGEL 305, the consumption of SEPIGEL 305 is 0～10mg/L.
5. high concentration methanol system olefin process wastewater treatment method as claimed in claim 4 is characterized in that: the consumption of SEPIGEL 305 is 0～5mg/L.
6. high concentration methanol system olefin process wastewater treatment method as claimed in claim 1 is characterized in that: during efficient anaerobic was handled, the N nutritive salt that adds was urea or ammonium chloride, and the P nutritive salt that adds is tsp or potassium primary phosphate.
7. high concentration methanol system olefin process wastewater treatment method as claimed in claim 1 is characterized in that: during efficient anaerobic was handled, outer circulation was carried out in the water outlet of internal recycle high efficiency anaerobic reactor, and recycle ratio is 0～50: 1.
8. high concentration methanol system olefin process wastewater treatment method as claimed in claim 7; It is characterized in that: when efficient anaerobic is handled; In the internal recycle high efficiency anaerobic reactor, inoculate with anaerobic grain sludge and handle waste water, the main control parameters that efficient anaerobic is handled is following:
(1) sludge concentration is 15～30g/L;
(2) the COD volumetric loading is 15～35kg/ (m
3D);
(3) reactor drum water outlet recycle ratio is 5: 1～10: 1;
(4) the anaerobic reaction temperature is 25～35 ℃;
(5) ratio of adding of N nutritive salt and P nutritive salt is COD: N: P-350～500: 5: 1.
9. high concentration methanol system olefin process wastewater treatment method as claimed in claim 1 is characterized in that: settling tank is set carries out postprecipitation when handling, the ST is 2～4h; The hydraulic surface loading of final settling tanks is 0.50～0.75m
3/ (m
2H).
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| CN103626358A (en) * | 2013-11-21 | 2014-03-12 | 中国科学院广州能源研究所 | Method for treating biodiesel wastewater |
| CN105439367A (en) * | 2014-06-18 | 2016-03-30 | 中国石油化工股份有限公司 | Methanol-to-olefin (MTO) wastewater processing apparatus and starting method thereof |
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| CN105439367A (en) * | 2014-06-18 | 2016-03-30 | 中国石油化工股份有限公司 | Methanol-to-olefin (MTO) wastewater processing apparatus and starting method thereof |
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