UASB type units are one in which no special media have to be used since the sludge granules themselves act as the 'media' and stay in suspension. UASB system is not patented. A typical arrangement of a UASB type treatment plant for municipal sewage would be as follows:
- Initial pumping
- Screening and degritting
- Main UASB reactor
- Gas collection and conversion or conveyance
- Sludge drying bed
- Post treatment facility
In the UASB process, the whole waste is passed through the anaerobic reactor in an upflow mode, with a hydraulic retention time (HRT) of only about 8-10 hours at average flow. No prior sedimentation is required. The anaerobic unit does not need to be filled with stones or any other media; the upflowing sewage itself forms millions of small "granules" or particles of sludge which are held in suspension and provide a large surface area on which organic matter can attach and undergo biodegradation. A high solid retention time (SRT) of 30-50 or more days occurs within the unit. No mixers or aerators are required. The gas produced can be collected and used if desired. Anaerobic systems function satisfactorily when temperatures inside the reactor are above 18-20°C. Excess sludge is removed from time to time through a separate pipe and sent to a simple sand bed for drying.
Size of Reactor: Generally, UASBs are considered where temperature in the reactors will be above 20°C. At equilibrium condition, sludge withdrawn has to be equal to sludge produced daily. The sludge produced daily depends on the characteristics of the raw wastewater since it is the sum total of (i) the new VSS produced as a result of BOD removal, the yield coefficient being assumed as 0.1 g VSS/ g BOD removed, (ii) the non-degradable residue of the VSS coming in the inflow assuming 40% of the VSS are degraded and residue is 60%, and (iii) Ash received in the inflow, namely TSS-VSS mg/l. Thus, at steady state conditions,
SRT= Total sludge present in reactor, kg
Sludge withdrawn per day, kg/d
= 30 to 50 days.
Another parameter is HRT which is given by:
HRT= Reactor volume, m3
Flow rate, m3/h
= 8 to 10 h or more at average flow.
The reactor volume has to be so chosen that the desired SRT value is achieved. This is done by solving for HRT from SRT equation assuming (i) depth of reactor (ii) the effective depth of the sludge blanket, and (iii) the average concentration of sludge in the blanket (70 kg/m3). The full depth of the reactor for treating low BOD municipal sewage is often 4.5 to 5.0 m of which the sludge blanket itself may be 2.0 to 2.5 m depth. For high BOD wastes, the depth of both the sludge blanket and the reactor may have to be increased so that the organic loading on solids may be kept within the prescribed range.
Once the size of the reactor is fixed, the upflow velocity can be determined from
Upflow velocity m/h = Reactor height
Using average flow rate one gets the average HRT while the peak flow rate gives the minimum HRT at which minimum exposure to treatment occurs. In order to retain any flocculent sludge in reactor at all times, experience has shown that the upflow velocity should not be more than 0.5 m/h at average flow and not more than 1.2 m/h at peak flow. At higher velocities, carry over of solids might occur and effluent quality may be deteriorated. The feed inlet system is next designed so that the required length and width of the UASB reactor are determined.
The settling compartment is formed by the sloping hoods for gas collection. The depth of the compartment is 2.0 to 2.5 m and the surface overflow rate kept at 20 to 28 m3/m2-day (1 to 1.2 m/h) at peak flow. The flow velocity through the aperture connecting the reaction zone with the settling compartment is limited to not more than 5 m/h at peak flow. Due attention has to be paid to the geometry of the unit and to its hydraulics to ensure proper working of the "Gas-Liquid-Solid-Separator (GLSS)" the gas collection hood, the incoming flow distribution to get spatial uniformity and the outflowing effluent.
A single module can handle 10 to 15 MLD of sewage. For large flows a number of modules could be provided. Some physical details of a typical UASB reactor module are given below:
||Rectangular or circular. Rectangular shape is preferred
||4.5 to 5.0 m for sewage.
|Width or diameter
To limit lengths of inlet laterals to around 10-12 m for facilitating uniform flow distribution and sludge withdrawal.
||gravity feed from top (preferred for municipal sewage) or pumped feed from bottom through manifold and laterals (preferred in case of soluble industrial wastewaters).
|Sludge blanket depth
||2 to 2.5 m for sewage. More depth is needed for stronger wastes.
||This is a deflector beam which together with the gas hood (slope 60) forms a "gas-liquid-solid-separator" (GLSS) letting the gas go to the gas collection channel at top, while the liquid rises into the settler compartment and the sludge solids fall back into the sludge compartment. The flow velocity through the aperture connecting the reaction zone with the settling compartmentt is generally limited to about 5m/h at peak flow.
||2.0-2.5 m in depth. Surface overflow rate equals 20-28 m3/m2/d at peak flow.
Process Design Parameters
A few process design parameters for UASBs are listed below for municipal sewages with BOD about 200-300 mg/l and temperatures above 20°C.
8-10 hours at average flow (minimum 4 hours at peak flow)
||30-50 days or more
|Sludge blanket concentration (average)
15-30 kg VSS per m3. About 70 kg TSS per m3.
|Organic loading on sludge blanket
||0.3-1.0 kg COD/kg VSS day (even upto 10 kg COD/ kg VSS day for agro-industrial wastes).
|Volumetric organic loading
||1-3 kg COD/m3 day for domestic sewage (10-15 kg COD/m3 day for agro-industrial wastes)
|BOD/COD removal efficiency
||Sewage 75-85% for BOD. 74-78% for COD.
||Minimum 1 point per 3.7-4.0 m2 floor area.
Either constant rate for pumped inflows or typically fluctuating flows for gravity systems.
||About 0.5 m/h at average flow, or 1.2 m/h at peak flow, whichever is low.
||0.15-0.25 kg TS per m3 sewage treated.
|Sludge drying time
||Seven days (in India)
||Theoretical 0.38 m3/kg COD removed. Actual 0.1-0.3 m3 per kg COD removed.
||Method of use is optional. 1 m3 biogas with 75% methane content is equivalent to 1.4 kWh electricity.
|Nutrients nitrogen and phosphorus removal
||5 to 10% only.