CN1055070C - Processing method of waste water from refined p-benzene dicarboxylic acid production - Google Patents
Processing method of waste water from refined p-benzene dicarboxylic acid production Download PDFInfo
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- CN1055070C CN1055070C CN96109791A CN96109791A CN1055070C CN 1055070 C CN1055070 C CN 1055070C CN 96109791 A CN96109791 A CN 96109791A CN 96109791 A CN96109791 A CN 96109791A CN 1055070 C CN1055070 C CN 1055070C
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- aerobic reactor
- level
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- sludge
- water
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- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 239000002351 wastewater Substances 0.000 title abstract description 16
- 238000004519 manufacturing process Methods 0.000 title abstract description 7
- 238000003672 processing method Methods 0.000 title 1
- 239000010802 sludge Substances 0.000 claims abstract description 35
- 238000000034 method Methods 0.000 claims abstract description 33
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 2
- 238000005111 flow chemistry technique Methods 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 40
- 238000010992 reflux Methods 0.000 abstract description 6
- 239000005416 organic matter Substances 0.000 abstract description 2
- 239000002994 raw material Substances 0.000 abstract description 2
- 239000003513 alkali Substances 0.000 description 8
- 239000002002 slurry Substances 0.000 description 4
- 239000000945 filler Substances 0.000 description 3
- 150000007524 organic acids Chemical class 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- KUCOHFSKRZZVRO-UHFFFAOYSA-N terephthalaldehyde Chemical class O=CC1=CC=C(C=O)C=C1 KUCOHFSKRZZVRO-UHFFFAOYSA-N 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 239000006260 foam Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 229910001415 sodium ion Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 235000010627 Phaseolus vulgaris Nutrition 0.000 description 1
- 244000046052 Phaseolus vulgaris Species 0.000 description 1
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 1
- 241000700141 Rotifera Species 0.000 description 1
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000002207 metabolite Substances 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 238000004804 winding Methods 0.000 description 1
Images
Classifications
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Activated Sludge Processes (AREA)
Abstract
The present invention relates to a two stage method for treating terephthalic acid high concentration production wastewater in an aerobic mode. A primary aerobic reactor and a secondary aerobic reactor are respectively provided with a sludge settling tank and a sludge refluxing system. When terephthalic acid production wastewater is treated by the present invention, COD in the wastewater can be reduced from 4000 to 10000 mg/l to below 100 mg/l, and can achieve the discharge standard; the organic matter volume load of the primary reactor reaches 8.0 kgCOD/m<3>. d, the organic volume load of the secondary reactor reaches 0.3 to 1.0 kgCOD/m<3>. d, and the pH of the raw material water can be reduced to 3.5 to 4.0.
Description
The invention belongs to a kind of treatment process of petrochemical complex high-concentration waste water, especially belong to a kind of pure terephthalic acid's high density production wastewater treatment method.
Organic concentration is higher in pure terephthalic acid (abbreviation PTA, the down together) factory effluent, mainly contains terephthalic acid (being called for short TA, down together), acetate and methyl acetate, and its concentration is respectively 400-1500mg/l, 1000-2000mg/l and 500-1000mg/l.COD in this waste water (organism integrated concentration, down together) can be up to about 10000mg/l, and PH is 3.0～4.0.Be one of more unmanageable waste water of generally acknowledging at present.Processing Chinese patent CN1039784 to this water proposes to adopt anaerobic-aerobic technology.After anaerobism and aerobic treatment, COD is about 400mg/l, and raw water concentration is lower than 2000mg/l.Among " water supply and drainage " Vol.22 No.2 " application of A/O biomembrance process in handling the chemical industry high-concentration waste water " introducing will be through the PTA waste water after the anaerobic-aerobic art breading, further adopt two sections anoxic-aerobic process, could be with the PTA production wastewater treatment to emission standard (below the COD 100mg/l).This process treatment PTA factory effluent flow process is longer.And anaerobic device requires, and air-tightness is good, need adopt filler, simultaneously triphase separator need be set, thereby the investment of equipment is improved.In addition, because anaerobic reaction has relatively high expectations the level of automation of device to the restriction of the scope of PH comparatively harsh (6.5-7.2), complicated operation, also higher to the requirement of technical level of operators.Contain a large amount of terephthaldehyde's acids materials in the PTA factory effluent, anaerobic process are lower to terephthaldehyde's acids material clearance, generally are lower than 50%.Therefore, discharge Na in the water
2CO
3Concentration is corresponding lower, and water outlet PH is also lower, is generally about 7.2-7.5.The recirculation water neutralising capacity is relatively poor, therefore requires the PH of water inlet to be at least 6.0.Because PTA factory effluent PH is lower, is generally 3.0-4.0, need adds a large amount of alkali neutralizations, thereby also make the anaerobic process cost higher.
The two-part high loading sewage water treatment method that Chinese patent CN 85 106350 A propose, flow process are by the fibrous packing contact-oxidation pool, aeration tank and solid-liquid separator are composed in series in proper order again.Do the contact oxidation technology of filler with fiber, in operational process, because biomembranous coming off makes water outlet all be subjected to bigger influence on turbidity and colourity.The part fiber hair with the microbial film piece come off, enter in pipeline and the valve, easily blocking pipeline.Fibrous packing is fixing difficult, and needs periodic replacement, and investment and process cost are raise.In addition, this patent is suitable for handling the water of low COD concentration, and introducing COD in the patent is 500-3300mg/l.And treating water is the waste water of easily degrading.Do not relate to the processing of wastewater of chemical industry with high concentration.
Chinese patent CN1123770A propose to adopt two sections aerobic method treatment PTA factory effluents, and aerobic and two sections aerobic orders are composed in series flow process by selector switch, one section.The returned sluge of raw water and one section aeration tank is mixed and enters selector switch, and the selector switch residence time is shorter, be generally 10-40 minute, and the COD concentration of former water is higher, is generally 1000-4000mg/l, and COD and organic acid are not degraded in selector switch basically.Because organic acid is not degraded in selector switch, potential basicity can't discharge, and the PH in the water does not raise, and the PH in the selector switch can not be lower than 6.0, therefore, requires the PH of former water can not be lower than 5.0.The PH of PTA factory effluent is generally 3.0-4.0, must add alkali former water PH is transferred to about 5.0, therefore needs to consume a large amount of alkali.In addition, adding alkali has promptly increased Na ion concentration, contains the TA (500-2000mg/l) of higher concentration in the PTA factory effluent, when the Na ion concentration in the former water is higher, and the Na in the water
+Also higher with the terephthalic acid na concn that terephthaldehyde's acid-respons generates.Para-phthalic sodium belongs to a kind of surfactant, and the microbe metabolite in the active sludge has certain viscosity, therefore, when drum air in reactor, forms a large amount of foams, and mud runs off with foam, also influences the normal running of device simultaneously.
The objective of the invention is to propose a kind of PTA waste water treatment process, overcome that prior art long flow path, investment are big, alkaline consumption reaches problems such as sludge loss greatly, simplify the operation course, improve sewage treating efficiency, particularly the COD in the high density PTA waste water directly is reduced to below the 100mg/l by 4000-10000mg/l.Its further purpose is to reduce alkali consumption, reduces mud discharging.
The present invention proposes a kind of two sections methods that aerobic flow processing PTA high density is produced waste water.The only 20-45 hour residence time.With this method treatment PTA factory effluent, can with the COD in the water, TA and acetate be reduced to 100mg/l, 10mg/l respectively by 4000-10000/1,400-1500 and 1000-2000mg/l respectively and below the 2mg/l.Reach emission standard.Raw water PH can be reduced to 3.0-4.0, need not add alkali, thereby saves process cost.
Main contents of the present invention comprise: flow process is made of in proper order one-level aerobic reactor, first grade subsides jar, secondary aerobic reactor and secondary slurry tank, the mud of first grade subsides jar is back to the one-level aerobic reactor, and the mud of secondary slurry tank is back in the secondary aerobic reactor.The excess sludge of first grade subsides jar is discharged to the secondary aerobic reactor.Be all active sludge in the firsts and seconds aerobic reactor, in the reactor except that being provided with gas distributor, facilities such as no filler.Service temperature in the firsts and seconds aerobic reactor is 15-40 ℃, and the sludge concentration in the one-level aerobic reactor is 3000-6000mg/l, and volumetric loading is 2.0-8.0kgCOD/m
3.d.Sludge concentration in the secondary aerobic reactor is 1500-3000mg/l, and volumetric loading is 0.1-1.0kgCOD/m
3.d.Dissolved oxygen in the aerobic reactor is 0.5-2.0mg/l.
Accompanying drawing 1 has been described technical process of the present invention:
(1) raw water homogeneous pond;
(2) one-level aerobic reactor;
(3) one-level sludge settling jar;
(4) secondary aerobic reactor;
(5) secondary sludge settling jar;
A～raw material waterline;
B～one-level aerobic reactor inflow hydrograph;
C～one-level aerobic reactor mud return wire;
D～one-level aerobic reactor goes out waterline;
E～first grade subsides jar goes out waterline;
F～secondary aerobic reactor mud return wire;
G～secondary aerobic reactor goes out waterline;
H～secondary slurry tank goes out waterline;
The outer winding displacement of i～first grade subsides jar excess sludge;
Be described with reference to the accompanying drawings process of the present invention: behind the high concentration Production of Terephthalic Acid waste water process homogeneous pond (1), enter one-level aerobic reactor (2). One-level aerobic reactor influent COD scope is 4000-10000mg/l, TA is 400-1500mg/l, sludge concentration is 2000-6000mg/l, the water outlet of one-level aerobic reactor enters one-level sludge settling tank (3) and carries out mud-water separation, a mud part is returned one-level aerobic reactor (2), another part enters secondary aerobic reactor (4), and the supernatant in the settling tank (3) enters secondary aerobic reactor (4). In secondary aerobic reactor (4), influent concentration is 200-600mg/l, sludge concentration is 1000-4000mg/l, the water outlet of secondary aerobic reactor (4) enters secondary settling tank (5), sludge reflux in the secondary settling tank (5) is in secondary aerobic reactor (4), and supernatant is discharged.
The interior organic matter degradation rate of one-level aerobic reactor (2) is very fast, and the COD more than 95%, TA and VFA are degraded. Because the organic acid degraded discharges sodium salt in the water, PH is increased to more than 8.5. Part is as recirculation water (reflux ratio is 1: 1), at raw water PH is in about 3.5 the situation, still can make former water PH rise to 7.0. Make former water in the situation that does not add alkali, the aerobe process is carried out smoothly. Thereby save a large amount of alkaline consumptions. Mud in the first grade subsides tank (3) turns back to one-level aerobic reactor (2). One-level aerobic reactor (2) internal volume load is higher, is about 2.0-8.0kgCOD/m3.d, COD concentration is 200-600mg/l, and the protozoan of sludge organism in mutually is mainly take beans shape worm and campanularian class as main. The mud of secondary settling tank (5) turns back to secondary aerobic reactor (4). Volumetric loading in the secondary aerobic reactor (4) is lower, is about 0.1-1.0 kgCOD/m3.d, COD concentration is below the 100mg/l, and sludge organism metazoa occurs in mutually, and take rotifers as main. The purpose that mud returns aerobic reactor separately is to keep different biofacies in two aerobic reactors, have higher treatment effeciency to guarantee one-level aerobic reactor (2), and secondary aerobic reactor (4) has the ability of advanced treating. Secondary aerobic reactor (4) volumetric loading is lower, and mud is in the endogenous respiration stage. Do not replenishing in the situation of mud, sludge quantity is on a declining curve. Therefore, the excess sludge with one-level sludge settling tank (3) little by little is discharged to as a supplement mud of secondary aerobic reactor (4). Make the residual sludge discharge of whole technical process less.
It is 4000-8000mg/l that the inlet COD concentration of one-level aerobic reactor of the present invention is fit to scope, and TA suitable concentration scope is 400-1200mg/l, and sludge concentration and volumetric loading preferably are respectively 3000-5000mg/l and 2.0-5.0kgCOD/m3.d. The influent concentration scope is advisable with 200-400mg/l in the secondary aerobic reactor, and sludge concentration and volumetric loading preferably are respectively 1500-3000mg/l and 0.1-0.3kgCOD/m3.d. The operating temperature of one-level and secondary aerobic reactor is preferably 20-35 ℃.
Because the present invention adopts two reactor mud return schemes respectively, makes two reactors remain different biophase, reasonable supplement and utilize active sludge.Cancelled selector switch, by the recirculation water pH value in the conditioned reaction device effectively, guaranteed the entire operation process steadily and efficient.Make that COD is reduced to below the 100mg/l by 4000-10000mg/l in the Production of Terephthalic Acid waste water.Volumetric loading in the one-level aerobic reactor can reach 2.0-8.0kgCOD/m
3.d, secondary aerobic reactor volumetric loading is 0.1-1.0kgCOD/m
3.d, terephthalic acid and VFA are reduced to 10mg/l by 800-1500mg/l and 1000-2000mg/l respectively and below the 2mg/l in the waste water, have avoided regulating the consumption that PH causes by adding alkali, and have too much discharged the secondary pollution that excess sludge causes.
Embodiment 1-4
PTA factory effluent COD concentration is 2000-10000mg/l, and PH is 3.5-4.5.One-level aerobic reactor (2) volume is 50 liters, and secondary aerobic reactor (4) volume is 30 liters.The PTA factory effluent directly enters one-level aerobic reactor (2), one-level aerobic reactor (2) water outlet enters first grade subsides jar (3), first grade subsides jar (3) water outlet enters secondary aerobic reactor (4), secondary aerobic reactor (4) water outlet enters secondary subsider (5), and secondary subsider (5) water outlet is directly discharged.The mud of first grade subsides groove (3) is back to one-level aerobic reactor (2), and reflux ratio is 1.0; The mud of secondary slurry tank (5) is back to secondary aerobic reactor (4), and reflux ratio is 0.5.Dissolved oxygen in the one-level aerobic reactor (2) is 1.0-2.0mg/l, and the dissolved oxygen of secondary aerobic reactor (4) is 2.0-2.5mg/l.The aerobic reactor service temperature is 15-40 ℃.Operation result sees the following form.
| Embodiment 1234 | |
| COD (mg/l) | Raw water 4,000 6,000 9,000 10000 one-level water outlets 200 300 450 600 secondary effluents 40 65 70 85 |
| TA (mg/l) | Raw water 400 700 1,300 1500 one-level water outlets 25 30 60 100 secondary effluents 58 10 15 |
| Volumetric loading (kgCOD/m 3.d) | A reactor 1.5 3.0 6.0 8.0 second reactors 0.1 0.4 0.8 1.0 |
| Dissolved oxygen (mg/l) | A reactor 1.5 1.6 1.4 1.0 second reactors 2.0 2.4 2.1 2.0 |
| Temperature ℃ | A reactor 18 30 40 24 second reactors 18 29 40 24 |
| Sludge concentration (mg/l) | A reactor 3,000 4,000 4,500 6000 second reactors 1,000 2,000 2,600 3000 |
| Reflux ratio | A reactor 1.0 1.0 1.0 1.0 second reactors 0.5 0.5 0.5 0.5 |
| PH | Former water 3.0 4.0 3.5 4.0 A reactors 8.5 8.7 8.7 8.8 second reactors 8.7 8.9 8.8 8.9 |
Claims (6)
1. the method for a two-stage aerobic flow processing pure terephthalic acid factory effluent, it is characterized in that technical process is made of in proper order following part: one-level aerobic reactor (2), one-level sludge settling jar (3), secondary aerobic reactor (4), secondary sludge settling jar (5), wherein the mud of one-level sludge settling jar (3) is back to one-level aerobic reactor (2), mud in the secondary sludge settling jar (5) is with flowing in the secondary aerobic reactor (4), the secondary aerobic reactor the insufficient sludge quantity mud of discharging by the one-level aerobic reactor provide, the service temperature of one-level and second reactor is 15-40 ℃, and dissolved oxygen is 0.5-3.0mg/l.
2. according to claim 1 method, it is characterized in that the service temperature in one-level and the secondary aerobic reactor is 20-35 ℃.
3. according to the method for claim 1, it is characterized in that the sludge concentration in the one-level aerobic reactor is 3000-6000mg/l, the sludge concentration in the secondary aerobic reactor is 1000-3000mg/l.
4. according to the method for claim 1, it is characterized in that the sludge concentration in the one-level aerobic reactor is 3000-5000mg/l, the sludge concentration in the secondary aerobic reactor is 2000-2500mg/l.
5. require 1 method according to claim, the volumetric loading that it is characterized in that the one-level aerobic reactor is 2.0-8.0kgCOD/m
3.d, the volumetric loading of secondary aerobic reactor is 0.1-1.0kgCOD/m
3.d.
6. require 1 method according to claim, the volumetric loading that it is characterized in that the one-level aerobic reactor is 2.0-5.0kgCOD/m
3.d, the volumetric loading of secondary aerobic reactor is 0.1-0.4kgCOD/m
3.d.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96109791A CN1055070C (en) | 1996-09-12 | 1996-09-12 | Processing method of waste water from refined p-benzene dicarboxylic acid production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96109791A CN1055070C (en) | 1996-09-12 | 1996-09-12 | Processing method of waste water from refined p-benzene dicarboxylic acid production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1176228A CN1176228A (en) | 1998-03-18 |
| CN1055070C true CN1055070C (en) | 2000-08-02 |
Family
ID=5120614
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96109791A Expired - Lifetime CN1055070C (en) | 1996-09-12 | 1996-09-12 | Processing method of waste water from refined p-benzene dicarboxylic acid production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1055070C (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1307109C (en) * | 2005-07-22 | 2007-03-28 | 中国石化仪征化纤股份有限公司 | Method for recovering aromatic carboxylic acid in waste water |
| CN101254985B (en) * | 2008-04-02 | 2010-06-02 | 中国纺织工业设计院 | PTA refined mother liquor reclaiming method and system |
| CN104276721A (en) * | 2013-07-08 | 2015-01-14 | 中石化洛阳工程有限公司 | Method for treating pure terephthalic acid production wastewater |
| CN111847768A (en) * | 2020-06-28 | 2020-10-30 | 魏毅宏 | Ion exchange resin production wastewater treatment system and method |
| CN111689654A (en) * | 2020-06-30 | 2020-09-22 | 新疆中泰创新技术研究院有限责任公司 | Sewage treatment system and method capable of reducing PTA anaerobic sludge feeding |
| CN114075017B (en) * | 2021-06-08 | 2024-09-10 | 中蓝连海设计研究院有限公司 | Biochemical treatment of high-salt wastewater from phenol-acetone production |
-
1996
- 1996-09-12 CN CN96109791A patent/CN1055070C/en not_active Expired - Lifetime
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| Publication number | Publication date |
|---|---|
| CN1176228A (en) | 1998-03-18 |
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