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A Lab Bench Scale Anaerobic Digester

A Lab Bench Scale Anaerobic DigesterJustin Ferrentino

David Harrison

Jacob KrallCEE 453

Fall 2004Table of Contents

2Table of Contents

3Abstract

3Objectives

3Introduction

4Methods

4Plant Configuration

4Reactor Process Control

5Results and Analysis

9Discussion

10Suggestions

11Appendix

Abstract

A lab bench scale anaerobic digestion system was created using activated sludge obtained from an anaerobic digester at the City of Ithaca Wastewater Treatment Plant. An anaerobic digester was set up in the lab to treat synthetic waste at a BOD concentration of 6500 mg/L and the system was automated using Process Controller software. Results showed that anaerobic digestion was indeed occurring in the system but suggested that many of the cells in the reactor were not viable. Future research should include investigating ways to maintain higher cell populations and treat a waste with a concentration closer to the typical wastewater BOD of 325 mg/L.Objectives

Our objective was to explore the use of anaerobic digestion for wastewater treatment with the use of a sequencing batch reactor. Synthetic waste was converted into methane and carbon dioxide gas, and vented out of the system. To ensure optimum growth conditions for the bacteria, the temperature of the reactor was maintained at 35C, and no oxygen was allowed in. We expected the treatment of the same volume of waste to be slower under anaerobic conditions than aerobic conditions, but the goal of this project is to lay some practical groundwork for further research projects in this area.

Introduction

The process of aerobic treatment of wastewater is well understood and widely used, but suffers from two severe drawbacks. These drawbacks are that it requires large amounts of energy to keep the reactor contents aerated, and that the process produces large volumes of sludge that must often be landfilled. Anaerobic digestion of wastewater is also widely used, as in the case of home septic tanks, but is not practiced at the municipal scale. Anaerobic digestion offers several advantages over aerobic digestion, in that it does not produce nearly as much sludge to be disposed of, and also that it yields energy in the form of methane gas. The drawbacks include that the digestion proceeds at a slower rate and that the bacteria favor temperatures of around 35C. Despite these challenges, if anaerobic bacteria cell concentrations in a reactor could be made high enough, unheated municipal waste water could be treated. This project attempts to start down that path.

Methods

Plant Configuration

Our plant was built around a 2.5 Liter glass jug with an inlet port at the bottom. The jug was placed on a hotplate, with a temperature probe placed on its exterior, and with a magnetic stirrer placed inside it. A rubber stopper with two holes was used to seal the top, while the influent line came in at the bottom port. The drain was made by a long steal tube that could be set to different heights to correspond to different recycle volumes (for a higher recycle volume, the drain pipe was simply set at a higher level). A Masterflex Model 7518-00 peristaltic pump with two drive heads and valves were used to both fill and drain the reactor. The pump flow rate was set at 2.88 mL/s. The drain valve was set at the desired height. In operation, the pump system worked by opening only the valve that was required, as in the case of filling the reactor where the influent valve would be opened, while the drain valve was left closed. On the influent end, a single line was run through the pump head by having one valve control tap water and one valve control the raw waste, but having both feed the same influent line. At the effluent end, waste was simply pumped out to a drain.

The only other major system for the reactor is the gas collection/regulation system. Gas regulation was achieved by having the second hole in the rubber stopper go to a second 2.5 Liter glass jug, with a 200 kilo Pascal pressure sensor measuring relative pressure between the gas collection jug and the atmosphere. The gas was vented to a vacuum line with the use of another valve, and the system was designed and run under a vacuum.

Figure 1: Process Schematic

Reactor Process Control

Our reactor was set up to be controlled via the Process Controller software. Below is a table outlining the states of our reactor and our exit conditions for the final reactor configuration.Table 1. States and control logic for anaerobic digester.

State NameExplanationExit Condition (state exiting to)

Fill With WastePump in 360 mL 20x waste to reactorTime>30 s (digestion startup)

Digestion StartupGas production begins; pressureTime>1/2 day (gas production) or

Allowed to build upGas Pressure>-10 kpa

(gas production)

Gas Productiongas production continues; Time>1 day (Settle) or

Pressure builds upGas Pressure>-10 kpa (gas vent)

Gas VentReactor vented to maintain vacuumGas Pressure 1 hr (Drain)

Drain360 mL drained from reactor via pumpTime> 10 min (fill with waste)

During the gas production, digestion startup and gas vent states, the reactor was kept at a temperature of 35C using PID with both the I and D terms set at 0. Using only the P term successfully kept the reactor very near the target temperature as the waste was being digested. The digestion startup and gas production states appear to be very similar. Digestion Startup was initially included to ensure that the reactor would be allowed to treat the waste long enough to produce enough methane to necessitate venting at least once. When it later became clear that given our volume of waste the reactor was unable to produce that volume of gas, the time condition was added to allow the reactor to leave the digestion startup state after one day. During much of our research, our reactor included a Fill with Water state in order to dilute the 20x waste. However, we chose to eliminate this state to allow our digester to treat a more concentrated waste.Results and AnalysisIn each cycle using our eventual reactor configurations, the reactor was given 0.0864 L of 6500 mg/L waste. We used several assumptions to obtain an approximation of the theoretical volume of gas that should be produced during the digestion: 1g of oxygen gas per gram of Carbonaceous Oxygen Demand (COD) and 1 mol of gas produced per mol of Carbon. Our calculation appears below:

Below we convert this value to an equivalent pressure produced (using a gas volume of 3L, equal to 1 full jug plus the volume of the second jug not filled with waste and solids):

For most of the duration of our experiment, we were operating the reactor believing (due to erroneous calculations) that the theoretical gas production was 0.11 mol, which influenced the duration which we allowed the reactor to produce gas. The following plot shows data obtained during a typical gas production phase for our reactor. It can be seen that there are three major regions in the graph. At first, the plot appears quite straightthe waste is being digested at an approximately constant rate. Then, as the amount of waste available decreases, the graph starts to curve and the slope becomes less steep. Finally, there is a second straight line region of the graph; this represents endogenous respiration by the cells after all waste has been digested. This plot gives a strong indication that there are two processes occurring that are producing gas: waste digestion and endogenous respiration.

Figure 2. Plot showing the gas production of the anaerobic digester for a period of slightly more than 1 day.

If we take the slope of the second line, consider this the rate of endogenous respiration and assume that this takes place at a constant rate throughout the cycle, then (1.132674days*13.450kPa/day)=15.234 kPa of gas production can be attributed to this process. This leaves the rest of the production, about 15 kPa of pressure, to digestion of the waste. This value is very close to theoretical value giving an indication that we are producing approximately our theoretical amount of gas. The following plot is similar to the previous one, but represents a cycle that was started immediately after adding additional cells to the reactor (after centrifuging raw sludge to concentrate them). Using the same analysis as above but using an endogenous respiration slope of 11.943 kPa/day (from the plot below), we attribute 11.7 kPa of gas production to digestion of the waste. This is closer to our theoretical value than is the value from the previous cycle, and it is fairly close to the previous value, strengthening the evidence that anaerobic digestion in our reactor is indeed occurring and is producing gas at approximately the rate we would expect. In addition to showing that anaerobic digestion is taking place, it is of that we added cells to the reactor between the trials shown in figures 1 and 2, but saw no increase (and in fact a decrease) in initial rate of gas production. The turbidity of the reactor was measured to be 320 NTUs, as compared with 350 NTUs for raw sludge obtained from the Ithaca anaerobic digester. This indicates that the cell concentration in the reactor remained significant and combined with the lack of effect on gas production rate after increasing cell concentration appeared to indicate that waste concentration was the limiting factor.

Figure 3. Plot showing Gas Production over a complete treatment cycle immediately after adding additional cells to the reactor.

However, in a further attempt to discover what parameter was limiting our methane production,