Low-Carbon Nitrogen and Phosphorus Removal System and Process for Sewage Treatment

Abstract

The disclosure belongs to the field of sewage treatment technology, in particular to a low-carbon nitrogen and phosphorus removal system and process for sewage treatment. The system of the disclosure includes a primary sedimentation fermentation tank, a mainstream modified A.sup.2O unit and a bypass anammox unit. The disclosure sets a denitrification phosphorus removal functional zone in the anoxic tank of the A.sup.2O system, and sets a deoxygenation zone in the aerobic tank. Combined with the primary sedimentation fermentation tank, the efficient utilization of the carbon source of the A.sup.2O process is strengthened. The system has good effluent quality and does not require the addition of a carbon source, and the aeration energy consumption is low, which achieves efficient and low-carbon nitrogen and phosphorus removal.

Claims

1. A low-carbon nitrogen and phosphorus removal system for sewage treatment, comprising a primary sedimentation fermentation tank (1), a mainstream modified A.sup.2O unit (13) and a bypass anammox unit (14), wherein the mainstream modified A.sup.2O unit (13) comprises a pre-anoxic tank (2), an anaerobic tank (3), an anoxic tank (4), an aerobic tank (5) and a secondary sedimentation tank (6); a water outlet of the primary sedimentation fermentation tank (1) is simultaneously connected with both the inlet end of the pre-anoxic tank (2) and the anaerobic tank (3), the outlet end of the pre-anoxic tank (2) is connected with the inlet end of the anaerobic tank (3), the outlet end of the anaerobic tank (3) is connected with the inlet end of the anoxic tank (4), the outlet end of the anoxic tank (4) is connected with the aerobic tank (5), the outlet end of the aerobic tank (5) is simultaneously connected with both the inlet end of the secondary sedimentation tank (6) and the inlet end of an internal reflux pump (10), the outlet end of the internal reflux pump (10) is connected with the inlet end of the anoxic tank (4), a bottom sludge outlet of the secondary sedimentation tank (6) is simultaneously connected with the inlet end of both a first sludge reflux pump (11) and a second sludge reflux pump (12), the outlet end of the first sludge reflux pump (11) is connected with the inlet end of the anoxic tank (4), and the outlet end of the second sludge reflux pump (12) is connected with the inlet end of the pre-anoxic tank (2); the bypass anammox unit (14) comprises a carbon source separation sedimentation tank (7) and an anammox tank (8), the inlet end of the carbon source separation sedimentation tank (7) is connected with the outlet end of a water inlet pump (9), the outlet end of the carbon source separation sedimentation tank (7) is connected with the inlet end of the anammox tank (8), the outlet end of the anammox tank (8) is connected with the inlet end of the anoxic tank (4), the bottom sludge outlet of the carbon source separation sedimentation tank (7) is connected with the inlet end of the anoxic tank (4), and the inlet end of the water inlet pump (9) is connected with the outlet end of the anaerobic tank (3); the anoxic tank (4) comprises a denitrification phosphorus removal zone (4a) and a denitrification nitrogen removal zone (4b), the inlet end of the denitrification phosphorus removal zone (4a) is simultaneously connected with the outlet end of the anaerobic tank (3), the bottom sludge outlet of the carbon source separation sedimentation tank (7), the outlet end of the anammox tank (8), the outlet end of the internal reflux pump (10) and the outlet end of the first sludge reflux pump (11), the outlet end of the denitrification phosphorus removal zone (4a) is connected with the inlet end of the denitrification nitrogen removal zone (4b), and the outlet end of the denitrification nitrogen removal zone (4b) is connected with the inlet end of the aerobic tank (5); the aerobic tank (5) comprises an aerobic zone (5a) and a deoxygenation zone (5b), the inlet end of the aerobic zone (5a) is connected with the outlet end of the denitrification nitrogen removal zone (4b), the outlet end of the aerobic zone (5a) is simultaneously connected with the inlet end of the deoxygenation zone (5b) and the secondary sedimentation tank (6), and the outlet end of the deoxygenation zone (5b) is connected with the inlet end of the internal reflux pump (10).

2. A low-carbon nitrogen and phosphorus removal process for sewage treatment, using the nitrogen and phosphorus removal system according to claim 1, wherein the process comprises the following steps: step S1: making a pretreated domestic sewage enter the primary sedimentation fermentation tank (1) for primary sedimentation and fermentation to provide carbon source for subsequent nitrogen and phosphorus removal; step S2: making one part of an effluent of the primary sedimentation fermentation tank (1) and one part of a reflux sludge of the secondary sedimentation tank (6) enter the pre-anoxic tank (2) for denitrification; step S3: making the other part of the effluent of the primary sedimentation fermentation tank (1) and an effluent of the pre-anoxic tank (2) enter the anaerobic tank (3) for biological phosphorus release; step S4: making one part of an effluent of the anaerobic tank (3) enter the carbon source separation sedimentation tank (7) for sludge water separation; step S5: making the supernatant of the carbon source separation sedimentation tank (7) enter the anammox tank (8) to complete the autotrophic nitrogen removal; step S6: making the sludge discharged from a bottom of the carbon source separation sedimentation tank (7), the internal reflux liquid from the internal reflux pump (10), the reflux sludge from the first sludge reflux pump (11), the effluent of the anammox tank (8) and the other part of the effluent of the anaerobic tank (3) simultaneously enter the denitrification phosphorus removal zone (4a) of the anoxic tank (4) for denitrification phosphorus absorption; step S7: making an effluent of the denitrification phosphorus removal zone (4a) successively enter the denitrification nitrogen removal zone (4b) of the anoxic tank (4) and the aerobic zone (5a) of the aerobic tank (5) to complete denitrification, aerobic phosphorus absorption and nitrification; step S8: making one part of an effluent of the aerobic zone (5a) enter the deoxygenation zone (5b) of the aerobic tank (5), and making an effluent of the deoxygenation zone (5b) enter the denitrification phosphorus removal zone (4a) through the internal reflux pump (10); step S9: after making the other part of the effluent of the aerobic zone (5a) enter the secondary sedimentation tank (6) to complete the sludge water separation, discharging the clear liquid from the outlet end of the secondary sedimentation tank (6); and step S10: making one part of a bottom sludge of the secondary sedimentation tank (6) enter the denitrification phosphorus removal zone (4a) through the first sludge reflux pump (11), and making the other part of the bottom sludge of the secondary sedimentation tank enter the pre-anoxic tank (2) through the second sludge reflux pump (12).

3. The low-carbon nitrogen and phosphorus removal process for sewage treatment according to claim 2, wherein a solid retention time in the primary sedimentation fermentation tank (1) is 1-5 days, and the hydraulic retention time is 0.5-1.0 hour; the surface loading is 2.0-2.5 m.sup.3/(m.sup.2.Math.h), a sludge blanket height in the primary sedimentation fermentation tank (1) is 60%-80% of the effective water depth, and the stirring power does not exceed 0.5 W/m.sup.3.

4. The low-carbon nitrogen and phosphorus removal process for sewage treatment according to claim 2, wherein the hydraulic retention time in the carbon source separation sedimentation tank (7) is 1-2 hours.

5. The low-carbon nitrogen and phosphorus removal process for sewage treatment according to claim 2, wherein the hydraulic retention time in the deoxygenation zone (5b) is 0.5-1.0 hour, with a stirrer or propeller inside, and the terminal dissolved oxygen (DO) is controlled at 0.5 mg/L or less.

6. The low-carbon nitrogen and phosphorus removal process for sewage treatment according to claim 2, wherein the anammox tank (8) is an integrated anammox system, which completes the nitritation and anammox processes in the same tank.

7. The low-carbon nitrogen and phosphorus removal process for sewage treatment according to claim 2, wherein the hydraulic retention time in the anammox tank (8) is 2-6 hours, when the activated sludge process is used, the solid retention time is 4-6 days, and the DO is 0.5 mg/L or less, when the pure membrane moving bed biofilm reactor (MBBR) process is used, the filler filling ratio is 30%-50%, and the DO is 0.5-2.5 mg/L.

Description

BRIEF DESCRIPTION OF FIGURES

[0038] FIG. 1 is the process flow diagram of the example of the disclosure.

[0039] Description of reference numerals: 1—primary sedimentation fermentation tank; 2—pre-anoxic tank; 3—anaerobic tank; 4—anoxic tank; 4a—denitrification phosphorus removal zone; 4b—denitrification nitrogen removal zone; 5—aerobic tank; 5a—aerobic zone; 5b—deoxygenation zone; 6—secondary sedimentation tank; 7—carbon source separation sedimentation tank; 8—anammox tank; 9—water inlet pump; 10—internal reflux pump; 11—first sludge reflux pump; 12—second sludge reflux pump; 13—mainstream modified A.sup.2O unit; and 14—bypass anammox unit.

DETAILED DESCRIPTION

[0040] In order to make the purpose, technical solution and advantages of the disclosure clearer, the disclosure is further described in detail in combination with the accompanying drawings and examples. It should be understood that the specific examples described here are only used to explain the disclosure and are not used to limit the disclosure.

[0041] As shown in FIG. 1, a low-carbon nitrogen and phosphorus removal system for sewage treatment, including a primary sedimentation fermentation tank 1, a mainstream modified A.sup.2O unit 13 and a bypass anammox unit 14;

[0042] the mainstream modified A.sup.2O nitrogen and phosphorus removal unit 13 includes a pre-anoxic tank 2, an anaerobic tank 3, an anoxic tank 4, an aerobic tank 5 and a secondary sedimentation tank 6;

[0043] the water outlet of the primary sedimentation fermentation tank 1 is simultaneously connected with both the inlet end of the pre-anoxic tank 2 and the anaerobic tank 3, the outlet end of the pre-anoxic tank 2 is connected with the inlet end of the anaerobic tank 3, the outlet end of the anaerobic tank 3 is connected with the inlet end of the anoxic tank 4, the outlet end of the anoxic tank 4 is connected with the aerobic tank 5, the outlet end of the aerobic tank 5 is simultaneously connected with both the inlet end of the secondary sedimentation tank 6 and the inlet end of an internal reflux pump 10, the outlet end of the internal reflux pump 10 is connected with the inlet end of the anoxic tank 4, the bottom sludge outlet of the secondary sedimentation tank 6 is simultaneously connected with the inlet end of both a first sludge reflux pump 11 and a second sludge reflux pump 12, the outlet end of the first sludge reflux pump 11 is connected with the inlet end of the anoxic tank 4, and the outlet end of the second sludge reflux pump 12 is connected with the inlet end of the pre-anoxic tank 2;

[0044] the bypass anammox unit 14 includes a carbon source separation sedimentation tank 7 and an anammox tank 8, the inlet end of the carbon source separation sedimentation tank 7 is connected with the outlet end of a water inlet pump 9, the outlet end of the carbon source separation sedimentation tank 7 is connected with the inlet end of the anammox tank 8, the outlet end of the anammox tank 8 is connected with the inlet end of the anoxic tank 4, the bottom sludge outlet of the carbon source separation sedimentation tank 7 is connected with the inlet end of the anoxic tank 4, and the inlet end of the water inlet pump 9 is connected with the outlet end of the anaerobic tank 3.

[0045] Particularly, the anoxic tank 4 includes a denitrification phosphorus removal zone 4a and a denitrification nitrogen removal zone 4b, the inlet end of the denitrification phosphorus removal zone 4a is simultaneously connected with the outlet end of the anaerobic tank 3, the bottom sludge outlet of the carbon source separation sedimentation tank 7, the outlet end of the anammox tank 8, the outlet end of the internal reflux pump 10 and the outlet end of the first sludge reflux pump 11, the outlet end of the denitrification phosphorus removal zone 4a is connected with the inlet end of the denitrification nitrogen removal zone 4b, and the outlet end of the denitrification nitrogen removal zone 4b is connected with the inlet end of the aerobic tank 5.

[0046] The aerobic tank 5 includes an aerobic zone 5a and a deoxygenation zone 5b, the inlet end of the aerobic zone 5a is connected with the outlet end of the denitrification nitrogen removal zone 4b, the outlet end of the aerobic zone 5a is simultaneously connected with the inlet end of the deoxygenation zone 5b and the secondary sedimentation tank 6, and the outlet end of the deoxygenation zone 5b is connected with the inlet end of the internal reflux pump 10.

EXAMPLE 2

[0047] A low-carbon nitrogen and phosphorus removal process for sewage treatment, and the process includes the following steps:

[0048] Step S1: The pretreated domestic sewage entered the primary sedimentation fermentation tank 1 for primary sedimentation and fermentation to provide carbon source, the inorganic components of suspended solids in sewage were removed, and the organic components was hydrolyzed while stripping from the outer layer of suspended particles to provide carbon source for subsequent nitrogen and phosphorus removal; and

[0049] the solid retention time in the primary sedimentation fermentation tank 1 was 1-5 d, and the hydraulic retention time was 0.5-1.0 h; and the surface loading was 2.0-2.5 m.sup.3/(m.sup.2h), the sludge blanket height in the primary sedimentation fermentation tank 1 was 60%-80% of the effective water depth, and the stirring power did not exceed 0.5 W/m.sup.3.

[0050] Step S2: One part of the effluent (0-30% of total water inlet amount) of the primary sedimentation fermentation tank 1 and one part of the reflux sludge (25-50% of total water inlet amount) of the secondary sedimentation tank 6 entered the pre-anoxic tank 2 for denitrification; and the nitrate in the reflux sludge was removed by denitrification to eliminate its adverse effect on the subsequent phosphorus release process in the anaerobic tank.

[0051] Step S3: The other part of the effluent of (70-100% of total water inlet amount) the primary sedimentation fermentation tank 1 and the effluent of the pre-anoxic tank 2 entered the anaerobic tank 3 for biological phosphorus release.

[0052] In the process of biological phosphorus release, dissolved organic matter was converted into VFA (volatile organic acid) by the fermentation of facultative bacteria, and then absorbed into the cells by polyphosphate accumulating bacteria to assimilate and synthesize intracellular carbon source storage PHB (poly-β-hydroxybutyrate).

[0053] Step S4: One part of the effluent (0-50% of total water inlet amount) of the anaerobic tank 3 entered the carbon source separation sedimentation tank 7 for sludge water separation; and the hydraulic retention time in the carbon source separation sedimentation tank 7 was 1-2 h.

[0054] Step S5: The supernatant of the carbon source separation sedimentation tank 7 had a very low content of dissolved organic matter and entered the anammox tank 8 to complete autotrophic nitrogen removal; and the anammox tank 8 was an integrated anammox system, which completes the nitritation and anammox processes in the same tank.

[0055] The hydraulic retention time in the anammox tank 8 was 2-6 h, when the activated sludge process was used, the solid retention time was 4-6 d, and the DO was 0.5 mg/L or less, when the pure membrane MBBR process was used, the filler filling ratio was 30%-50%, and the DO was 0.5-2.5 mg/L.

[0056] Step S6: The sludge discharged from the bottom of the carbon source separation sedimentation tank 7, the internal reflux liquid from the internal reflux pump 10, the reflux sludge from the first sludge reflux pump 11, the effluent of the anammox tank 8 and the other part of the effluent (0-50% of total water inlet amount) of the anaerobic tank 3 simultaneously entered the denitrification phosphorus removal zone 4a of the anoxic tank 4 for denitrification phosphorus absorption.

[0057] The sludge discharged from the bottom of carbon source separation sedimentation tank 7 was rich in PHB, in the anoxic stage, denitrification polyphosphate accumulating bacteria used NO.sub.3.sup.− in the internal reflux liquid as an electron acceptor to oxidize PHB, the dissolved phosphate in the effluent of anammox tank 8 and the other part of effluent of the anaerobic tank 3 were excessively absorbed, and NO.sub.3.sup.− was reduced to nitrogen at the same time.

[0058] Step S7: The effluent of the denitrification phosphorus removal zone 4a successively entered the denitrification nitrogen removal zone 4b of the anoxic tank 4 and the aerobic zone 5a of the aerobic tank 5 to complete denitrification, aerobic phosphorus absorption and nitrification.

[0059] Step S8: One part of the effluent (10-30% of total water inlet amount) of the aerobic zone 5a entered the deoxygenation zone 5b of the aerobic tank to remove DO in the internal reflux liquid, which had an impact on denitrification in the anoxic zone, and the effluent from the aerobic tank's anaerobic zone 5b entered the denitrification phosphorus removal zone 4a via the internal reflux pump 10.

[0060] The hydraulic retention time in the deoxygenation zone 5b was 0.5-1.0 h, with a stirrer or propeller inside, and the terminal DO was controlled 0.5 mg/L or less.

[0061] Step S9: After the other part of the effluent (70-90% of total water inlet amount) of the aerobic zone 5a entered the secondary sedimentation tank 6 to complete the sludge water separation, the clear liquid was discharged from the outlet end of the secondary sedimentation tank 6.

[0062] Step S10: One part of the bottom sludge (25-50% of total water inlet amount) of the secondary sedimentation tank 6 entered the denitrification phosphorus removal zone 4a through the first sludge reflux pump 11, and the other part (25-50% of total water inlet amount) of the bottom sludge of the secondary sedimentation tank entered the pre-anoxic tank 2 through the second sludge reflux pump 12.

[0063] Finally, it should be explained that the above detailed descriptions are only for purposes of illustration of the technical solution of the disclosure and are not intended to be limiting. Although the disclosure is described in detail with reference to examples, those ordinary skilled in the art should understand that the technical solution of the disclosure can be modified or equivalently replaced, without departing from the spirit and scope of the technical solution of the disclosure, which should be covered in the claim scope of the disclosure.