Multi-Stage Declined Aeration Promoting Partial ... · PDF filenamed partial nitrification is...

Reactor

Xiaolan Zeng, Xuebin Hu, and Wenchuan Ding Three Gorges Reservoir Area’s Ecology and Environment Key Laboratory of Ministry of Education, Chongqing

University, Chongqing, 400045, China

Email: [email protected], [email protected], [email protected]

Dan Wu Department of Resource Exploration and Civil Engineering, Chengdu University of Technology, Chengdu, 610059,

China

Email: [email protected]

Abstract—To optimize partial nitrification process, a

modified Multi-stage Declined Aeration strategy in a

sequencing batch biofilm reactor (SBBR) was developed.

The experiments were carried out with low total organic

carbon to nitrogen (C/N) ratio (3.8-5.7) synthetic wastewater

at temperature of 29±1°C under three different aeration

modes. The results showed that oxidation of ammonia to

nitrite and simultaneous nitrification and denitrification

(SND) in a SBBR system successfully achieved under low

DO concentration condition (≈0.8 mg·L-1). Nitrite

accumulation rate (NAR) under three modes CA, SDA1 and

SDA2 were 91.1%, 88.3% and 100.0%, while SND efficiency

were 63.4% , 69.5% and 74.7%, respectively. Three-stage

Declining Aeration (SDA2 mode) was the best strategy with

a complete partial nitrification in SBBR reactor. Meanwhile,

SDA2 could save aeration flux by 6% and increase TN

removal rate by 10% in comparison to Continuous Aeration

(CA) during the aeration phase. It is speculated that

anaerobic ammonium oxidation (ANAMMOX) process

could be involved in TN removal via SND during the

aeration period in SBBR system. The results suggest that

Multi-stage Declined Aeration strategy is an alternative

aeration approach to promote partial nitrification in a

biofilm system.

Index Terms—partial nitrification, Dissolved oxygen (DO),

Sequencing batch biofilm reactor (SBBR), Multi-stage

declining aeration, Nitrite accumulation rate (NAR),

I. INTRODUCTION

A typical biological process for nitrogen removal from

wastewater includes nitrification and denitrification. In

the process of nitrification, ammonia is oxidized to nitrate

via nitrite by ammonia oxidizing bacteria (AOB) and

nitrite oxidizing bacteria (NOB) under aerobic condition.

Subsequently, this nitrate is reduced to gaseous nitrogen

by the denitrifying bacteria in the presence of sufficient

organic carbon as electron donors under oxygen

exclusion condition. However, many municipal

Manuscript received June 3, 2014; revised September 13, 2014.

wastewater treatment plants (WWTPs) in China,

especially those employed in rural area, are currently

characterized their influent water by organic carbon

deficiency and ammonia overload. The addition of

external organic matter are needed for those WWTPs to

complete the conventional denitrification process which

results in increasing of operation costs. Therefore, it is

necessary to develop cost-effective technologies for

nitrogen removal in wastewater of low total organic

carbon to nitrogen (C/N) ratio.

Short-cut nitrification and denitrification has been

observed that ammonium can be converted to nitrite

during ammoxidation by AOB, and then, the produced

nitrite in combination with free ammonium will be

transformed to gaseous nitrogen without the supply of

organic carbon, which is referred to anaerobic ammonium

oxidation (ANAMMOX). These processes theoretically

lower oxygen demand up to 25% in ammonia oxidation

and decrease 40% of organic carbon consumption for

subsequent heterotrophic denitrification in comparison

with conventional nitrogen removal process. It also

presents advantages of reducing sludge generation and

reaction time [1]. So it has been raised concerns to be

technologically feasible for low C/N ratio wastewater

treatment [2]-[4]. The crucial step in these processes

named partial nitrification is to suppress nitrite oxidation

without inhibition of ammoxidation activity, i.e., to

terminate the oxidation of ammonium to nitrite [5]. Many

factors such as dissolved oxygen (DO) concentration [6]-

[10], temperature[11], [12] and hydraulic retention time

(HRT) [13] were reported that could regulate the

accumulation of nitrite during nitrification. Aeration

control was considered to be a priority due to its

advantages of saving energy, flexible controlling mode

and broad application in different biological wastewater

treatment systems [14].

There were two kinds of aeration control strategies

commonly used for partial nitrification system. The

1

Journal of Life Sciences and Technologies Vol. 2, No. 1, June 2014

2014 Engineering and Technology Publishing

Multi-Stage Declined Aeration Promoting Partial

doi: 10.12720/jolst.2.1.1-7

Nitrification in a Sequencing Biofilm Batch

[2], free ammonia (FA) concentration [9], [8], pH value

continuous aeration strategy kept aeration at a constant

airflow rate throughout the aeration period. It had been

applied to partial nitrification system in all kinds of

reactors [15]-[17]. When oxygen concentration below 0.5

mg·L-1, the nitrite oxidation rate decreased more than the

ammonia oxidation rate, thus occurred nitrite

accumulation [8]. But low DO concentration generally

not only reduced the activity of AOB but also resulted in

sludge bulking [18], [19]. The intermittent aeration

strategy switched aeration and non-aeration periodically

to create anaerobic/anoxic conditions. It currently used to

facilitate nitrogen removal [20]. But under intermittent

aeration process, a portion of nitrate was produced in

effluent so that extra organic carbon was needed for total

nitrogen removal via heterotrophic denitrification.

Based on the results of our previous work, high air flux

was needed in the early aeration stage to meet the

requirement of DO consumption for COD degradation

and ammonification by heterotrophic bacteria. Thereafter,

decreased airflow would be more beneficial to inhibit

activity of NOB and achieve high nitrite accumulation

rate (NAR) in the end of aeration. In this paper, a

modified continuous aeration mode named Multi-stage

Declined Aeration (MSDA) was proposed to improve the

performance of partial nitrification. A lab-scale

sequencing biofilm batch reactor (SBBR) was used to

investigate the performance of short-cut nitrification

denitrification under different aeration strategies: constant

aeration (CA), two-section declining aeration (SDA1) and

three-section declining aeration (SDA2). The objectives

of this study are to: (i) investigate the performance of

partial nitrification, (ii) evaluate energy consumption

under new aeration strategy comparing with traditional

continuous aeration strategy.

II. MATERIALS AND METHODS

A. Laboratory-Scale Reactor

A laboratory-scale SBBR system with an working

volume of 12.0 L was used for the study. The cylindrical

reactor was made of polyvinylchloride, with an internal

diameter of 200 mm and a height of 600 mm. The reactor

was filled with multiple layers flexible plastic fiber

carriers (30% v/v) and the theoretical surface area of

2600 m2·m

-3. For each layer, the fibrous carriers were

fixed on a plastic discs with diameter of 150 mm. The

aeration system was composed of one air pump and two

porous stone air diffusers, and the air flow rate was

regulated by an flowmeter. Three peristaltic pumps were

used. The first one pumped wastewater into the reactor

from a storage tank during the fill phase. The second one

discharged the effluent from the reactor during the draw

phase. The last one circulated the water in the tank for

mixing. The temperature in the reactor was kept at

29±1°C with an adjustable heater.

B. SBBR Operation and Synthetic Wastewater

Preparation

The duration of a complete cycle was 480 min, giving

three cycles per day. In each cycle, the reactor was

operated with instantaneous FILL, 5.5h AERATION,

1.5h MIXING, 0.5h SETTLE and 0.5h DRAW/IDLE.

Three different aeration modes were adopted during the

period of experiment. CA mode was continuous aeration

at a constant airflow rate of 12.0 L·h-1

in aeration phase

of each cycle (Fig. 1(a)). SDA1 mode was two-stage

aeration at an airflow rate of 15.6 L·h-1

lasting 1.5h with a

following airflow rate of 12.0 L·h-1

lasting 4.0h (Fig.

1(b)). SDA2 mode separated aeration phase into three

sequential stages at an airflow rate of 15.6 L·h-1

lasting

1.5h, an airflow rate of 12.0 L·h-1

lasting 2.0h and an

airflow rate of 7.2 L·h-1

lasting 2.0h, respectively (Fig.

1(c)). At the end of each cycle, 6.0 liter of treated effluent

was decanted by a peristaltic pump and the same volume

of feeding solution was pumped into the reactor at the

beginning of next cycle. The SBBR system ran

automatically by a PLC programmable logic control to

manipulate the pumps.

0 60 120 180 240 300 360 420 480

Time

(min)

Fill Draw

QL=15.6L·h-1 QL=12.0L·h-1QL=7.2L·h-1

Three-section Declined Aeration (SDA2)

Fill Draw

QL=15.6L·h-1 QL=12.0L·h-1

Two-section Declined Aeration (SDA1)

Fill DrawConstant Aeration (CA)

Aeration Non-aeration Settle Idle

QL=12.0L·h-1

(c)

(b)

(a)

Figure 1. Sequencing operation of the SBBR system

The seed sludge was collected from an aerobic tank at

the Tangjiatuo Wastewater Treatment Plant in Chongqing,

China. Before this experiment was conducted, the SBBR

system had run 120 days and undergone four stages (data

are not shown): start-up (30 days, Days 1-30), a constant


during aeration phase (40 days,

Days 31-60), a constant airflow rate of 15.6 L·h-1

during

aeration phase (30 days, Days 61-90), a constant airflow

rate of 7.2 L·h-1

during aeration phase (30 days, Days 91-

120). The synthetic wastewater was prepared to simulate

the practical domestic wastewater by mixing the

following composition (mg·L-1

) into tap water: glucose

(63), soluble starch (37), NH4Cl (175), peptone (250),

yeast extract (50), KH2PO4 (8), Na2CO3 (350) and 1mL

of trace elements solution. The composition of trace

elements solution was based on Ruiz et al. (2003). The

main characteristics of synthetic wastewater were: COD

350.0±50.0 mg·L-1

, NH4+-N 67.5±7.5 mg·L

-1, TN 77.0

±9.0 mg·L-1

, TP 4.5±1.2 mg·L-1

, pH 8.5±0.3, C/N 3.8-

5.7.

C. Analysis Methods

NH4+-N, NO2

--N, NO3

--N and TN were measured with

a UV-VIS spectrophotometer (Beijing Persee Corp.,

China) in accordance with the standard APHA methods

[21]. COD was measured using Hach COD-kits (Hach,



USA). DO and pH were measured with a JPBJ-608 DO

meter (Heng Odd Inc., China) and a PHS-25B pH meter

(Dapu Inc., China), respectively. The NAR, SND

efficiency and the TN removal rate were calculated

according to the following equations [22], [23]:

%100--

-

32

2

NNONNO

NNONAR

(1)

%100

-

-- %

)(4

ox4

oxidized

producedxidized

NNH

NNONNHSND

(2)

%1001%

initial

final

TN

TNTN

(3)

A. Performance of the SBBR System

The study lasted 45 days and separated with three of

15d period for each aeration mode. The suspended sludge

in the SBBR reactor was negligible because released flocs and detached biofilm were discharged out of the

reactor in the draw phase each day. So the effluent quality

was tested directly without clarification. The overall

performance of the reactor is shown in Fig. 2. The mean

value of measurement in last 10 day runs of each aeration

mode was calculated because the SBBR system could run

stably after aeration mode changing 5 days. Effluent

COD concentration revealed that the average COD

removal rate were 92% (CA), 91% (SDA1) and 89%

(SDA2), respectively (Fig. 2(A)). The data are similar to

other partial nitrification systems [24], [25]. The effluent

COD concentration was mostly below 40 mg·L-1

in each

mode which was satisfied by Chinese national discharged

standard of pollutants for municipal wastewater treatment

plant. As the average DO concentration during the

aeration phase under CA, SDA1 and SDA2 mode was

less than 0.8 mg·L-1

, it indicated that low DO concen-

tration in solution was sufficient to the requirement of

oxygen consumption for organic matter degradation.

Figure 2. The performances of the SBBR system.

The ammonium oxidation in SBBR system is shown in

Fig. 2 (B). NO2--N concentration in effluent was much

higher than NO3--N concentration of each aeration mode

indicating dominant partial nitrification during aeration


III. RESULTS AND DISCUSSION


period. The average NAR calculated according to

equation (1) of the mode CA, SDA1 and SDA2 at the end

of aeration were 91.1%, 88.3% and 100.0%, respectively.

The results suggest fully partial nitrification could

achieve in a SBBR system under specific aeration

strategy. It could be seen in Fig. 2 (C), the average NH4+-

N removal rates of the system of three modes were 90% ,

98% and 94%, respectively. Lim et al [26] suggested that

about 11-14% of NH4+-N was removed by the process of

biological assimilation. So the most of NH4+-N removal

was carried out through ammonium oxidation. The

average TN removal rates of the SBBR system were

75.5% (CA), 75.3% (SDA1) and 79.8% (SDA2),

respectively. But it was measured that the average TN

removal rates were 69.1%, 73.5% and 76.1% at the end

of aeration phase, i.e., the most of TN removal was

completed during the aeration phase. The data

demonstrate occurrence of SND in SBBR system during

aeration which was reported by other researches [3], [28],

[28]. The mean values of SND efficiency calculated

according to equation (2) were 63.4% (CA), 69.5%

(SDA1) and 74.7% (SDA2), respectively. Given that both

ammonium and nitrite concentrations in effluent

decreased further in non-aeration (mixing) phase, it

suggest that the rest TN removal could be attributed to

anaerobic ammonium oxidation (ANAMMOX) [29] in

anoxic condition.

B. Nitrogen Conversion in a Cyclic Operation

To investigate nitrogen conversion under Multi-stage

Declined Aeration mode in the SBBR system, variations

of nitrogen species, COD and control parameters

including DO and pH in a typical cycle operation were

measured on the same day of each aeration mode. It

could be seen in Fig. 3, the NH4+-N concentration

presented its highest level after the instantaneous fill,

because NH4Cl was added in the synthetic wastewater as

a source of resolvable nitrogen. Thereafter, the NH4+-N

concentration decreased linearly and the NO2--N

concentration increased linearly similar to intermittent

aeration strategy [21]-[26]. The means of NH4+-N

oxidation rate of 15.6 L h-1

under SDA1 and SDA2 mode

were 8.7 mg·(L·h)-1

and 8.5 mg·(L·h)-1

at the first 90min,

which were higher than 5.1 mg·(L·h)-1

of CA with the


. Then the NH4+-N oxidation rate

of SDA1 and SDA2 decreased to 5.2 mg·(L·h)-1

and 5.6

mg·(L·h)-1

closing to CA (5.1 mg·(L·h)-1

), while each of

aeration mode had the same airflow rate of 12.0 L h-1

in

the mid aeration period (90-210min). In the last of

aeration period (210-330min) under SDA2 mode, the

airflow rate dropped to 7.2 L·h-1

and the corresponding

NH4+-N oxidation rate was 3.7 mg·(L·h)

-1 which was

lower than that of the CA mode. The data suggest the

positive correlation between NH4+-N conversion

efficiency and aeration density.

The COD concentration was observed dropping to

around 60 mg·L-1

at the first 90min of aeration period in

three aeration modes and then decreased gently. It

indicates most COD degradation completed in a very

short period when the most amount of DO was consumed

at the beginning of aeration phase. Laanbroek et al. [30]

revealed that the metabolic activities of heterotrophic

bacteria AOB and NOB needed the participation of

dissolved oxygen, but AOB and NOB had no competitive

advantages for dissolved oxygen utilization with

heterotrophic bacteria in lack of dissolved oxygen

condition. In this study, SDA1 and SDA2 mode adopted

an airflow rate of 15.6 L·h-1

at the beginning 90 minutes,

which was higher than that of CA (12.0 L·h-1

) , resulting

in the higher NH4+-N oxidation rate in the beginning and

the higher overall NH4-N removal rate during aeration

period than that of CA. Therefore, it could be proved that

large airflow at the beginning of the aeration phase would

promote ammonium oxidation reactions.

Figure 3. Typical profiles of nitrogen species in different cycles

Along with NH4+-N concentration decreasing due to

nitrification, NOB obtained ample substrate of NO2--N

and advantage of DO concentration for nitrite oxidation.

It was considered that nitrification was shifted to the

support of nitrite oxidation progress from ammonium



oxidation progress [31], [32]. As shown in Fig. 3, when

the airflow rate was above 12.0 L·h-1

, the nitrate was

produced via nitrite oxidation under each aeration mode.

The mode SDA1 had the highest NO3--N concentration in

effluent with the largest total volume of air input (71

L·cycle-1

versus 66 L·cycle-1

to CA and 62 L·cycle-1

to

SDA2) into the reactor during the aeration phase among

three modes. The result is in accordance with previous

studies that over aeration would lead to more NO3--N

production in solution and partial nitrification

deterioration [14]. But the airflow rate of 7.2 L·h-1

adopted by SDA2 mode at the last 120 minutes during the

aeration phase presented the nearly 100% of NAR,

namely no nitrate was produced. The result suggests that

small airflow could effectively inhibit the conversion

from NO2--N to NO3

—N, and enhance SND in this stage

which increased SND by 10% in comparison with CA

mode. Therefore, it could be concluded that small airflow

in the late of aeration period would facilitate to

development of partial nitrification.

The cyclic variations of DO concentration in SBBR

system, which is shown in Fig. 4, could reveal the oxygen

balance for organic substance degradation and nitrogen

conversion during one cycle operation. Under each mode,

the DO dropped to less than 0.1 mg·L-1

after the

instantaneous fill and increased linearly up to around 0.8

mg·L-1

in the subsequent 90 minutes of aeration, and then

the DO concentration increasing slowed down during the

rest aeration period. The DO increasing trend

synchronizing with COD concentration decreasing trend

(Fig. 3) indicates oxygen consumption was dominated by

organic substance degradation at the beginning of the

aeration phase.

Figure 4. Typical profiles of DO and pH in a complete cycle

Then, the ammonium oxidation reaction was

responsible for the primary oxygen consumption in

reactors. The solution pH decreased during the aeration

period was attributed to nitrification. It could be seen in

Fig. 3 and Fig. 4, the performances of partial nitrification

in SBBR system during aeration phase greatly depended

on variation of DO concentration of each aeration mode.

Especially in the last 120 minutes aeration period (210-

330min), the DO concentration under CA and SDA1

modes increased fast indicating oxygen supplied by

aeration excessive to oxygen consumed by nitrification.

Thus the NO3--N concentration increased in the end of

aeration under CA and SDA1 modes due to partial

nitrification deterioration. On the contrary, the DO

concentration increased more gently under SDA2 (Fig.

3C) when the airflow rate decreased to 7.2 L·h-1

resulting

in no nitrate production.

As mentioned before, SND was observed in SBBR

system under three aeration modes similar to other

reports [3]-[31]. It was because the diffusion resistance of

DO towards the inner zone of the biofilm increased with

the depth of biofilm resulting in anoxic zone existence

inside the biofilm during aeration. Münch et al. [33]

suggested DO concentration around 0.5 mg·L-1

was

suitable to achieve complete SND for SBR system. But in

this study, over 60% SND efficiency achieved under

average DO concentration around 0.8 mg·L-1

(Fig. 3).

The experimental results indicate that the suitable DO

concentration for complete SND in biofilm or attached

growth systems could be higher than that of in suspended

growth systems. The COD concentration had only slight

decrease suggested that organic substance degradation

had been completed after 90 minutes aeration (Fig. 3).

That means no sufficient organic carbon to be used for

reduction of nitrite and nitrate produced in the aeration

phase to gaseous nitrogen by heterotrophic denitrification.

Therefore, it is implied that ANAMMOX process could

be the alternative pathway for TN removal via SND

during the aeration period in SBBR system.

IV. CONCLUSION



(1) Partial nitrification and SND in a SBBR system for

low C/N wastewater treatment were successfully

achieved under low DO concentration condition (≈0.8

mg·L-1

).

(2) Multi-stage Declining Aeration strategy owned

higher NH4+-N removal rates (98% to SDA1 and 94% to

SDA2) and SND efficiency (69.5% to SDA1 and 74.5%

to SDA2) in aeration phase than that of Conventional

Constant Aeration strategy (90% and 63.4% to CA).

(3) Three-stage Declining Aeration mode (SDA2) was

the best strategy for partial nitrification in SBBR reactor

with 100% NAR obtained. Meanwhile, SDA2 could save

aeration flux by 6% and increase TN removal rate by 6%

in comparison to Conventional Constant Aeration

strategy (CA).

ACKNOWLEDGMENT

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The authors gratefully acknowledge financial support

from the Water Pollution Control and Management of

Major Special Science and Technology in China (Project

number 2012ZX07102-001-04), the Scientific and

Technical Innovation Project of Chongqing University

Graduation Foundation in China (Project number

CDJXS11210015) and the support of K.C. Wong

Education Foundation, Hong Kong.

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Wenchuan Ding was born in Chengdu, the capital of Sichuan Province, mainland of

China in 1969. He received his Ph.D degree

from Chongqing University in municipal engineering in 2007. His major field of study

was wastewater treatment and solid waste management.

He is currently a professor in the School of

Urban Construction and Environmental Engineering at Chongqing University. He has

been working in the areas of 1) biochar for wastewater treatment and contaminated lands remediation, 2) trace elements control in water and

sediment, and 3) the recycling of biosolids and other residuals derived

from agricultural, industrial, and municipal activities. Prof. Ding is China National Association of Engineering Consultants

(Registered Consulting Engineer, Specialist of Chongqing Science & Technology Consulting Center, the Chinese Institute of Certified Public

Accountants, and the member of Chongqing Science & Technology

Association.



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