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8/19/2019 Saleem India Blog

1/16

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P E O P L E F R O M D I F F E R E N T P A R T S O F I N D I A . A R E Y O U I N T E R E S T E D T OP A R T N E R W I T H M E . P L E A S E C A L L M E A T 9 8 9 9 3 0 0 3 1 O R L E A V E A

M E S S A G E A T S A L E E M A S R A F ! G M A I L . C O M . I H A V E C O L L E C T E DA R T I C L E S I F O U N D I N T E R E S T I N G H E R E S O T H A T I C A N R E A D T H E MA T M Y L E I S U R E . 9 0 " O F T H E P O S T S A R E N O T W R I T T E N # Y M E .

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S E A R C H T H I S B L O G

T H U R S D A Y , D E C E M B E R 0 3 , 2 0 1 5

Desig !" UASBR U#"$!% A&e'!(i) S$*+ge B$&e- Re&)-!'

These are the 4 to a!"#at"o$s o% the UASB rea#tors&

o Breweries and beverage industry

o Distilleries and fermentation industry

o Food Industry, Slaughter Houses.

o Pulp and paper

To'ether, these %o(r "$)(str"a! se#tors a##o($t %or *+ o% the a!"#at"o$s- Ho.e/er, the

a!"#at"o$s o% the te#h$o!o' are ra")! ea$)"$', "$#!()"$'&

1- treate$t o% #he"#a! a$) etro#he"#a! "$)(str e%%!(e$ts

2- tet"!e "$)(str wastewater

3- !a$)%"!! !ea#hates

4- Co$/ers"o$s "$ the s(!%(r ##!e a$) reo/a! o% eta!s-

Search

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2/16

YOU NEED AN EXPERT WITH SPECIFIC INDUSTRY WISE EXPERIENCE TO

DESIGN A PROPER UASBR SYSTEM.

The UASB reactor can be designed as circular or rectangular. Modular design can be preferred

when the volume of reactor exceeds about 400 m. !t is necessar" to select proper range of

operating parameters for design# such as# $% S% superficial li'uid upflow velocit" (referred as

li'uid upflow velocit")# and *&T. The literature recommendations for all these parameters and

design procedure to account these recommendations are given below.

What is Upfow Anaerobic Sludge Blanket?

Upflow anaerobic sludge blanket, or UASB, is a form of anaerobic (oxygen-free)

digester used in wastewater treatment !t is a methane-produing digester which

uses an anaerobic process and forming a blanket of granular sludge and is

processed by anaerobic microorganism

UASB was de"eloped in #$%&s by 'etinga in the etherlands !t is essentially a

suspended growth system in which proper hydraulic retention time

(HR! and organic loading rate ("#R! is maintained in order to facilitate the

dense biomass aggregation known as granulation

http://www.iwawaterwiki.org/xwiki/bin/view/Articles/UpflowAnaerobicSludgeBlanketReactor?language=http://www.iwawaterwiki.org/xwiki/bin/view/Articles/UpflowAnaerobicSludgeBlanketReactor?language=


3/16

How to $esign UASB %ond

About a week ago, ! asked the appointed "endor who will design and supply

wastewater treatment unit about design calculation of UASB pond he design of

UASB pond is a function of* !"D input of wastewater

Flow of wastewater

"rgani loading rate

Hydrauli retention time

"rganic loading rate is a measure of the biological con"ersion capacity of

the anaerobic digestionsystem !t is expressed in kg +hemical xygen emand

(+) or .olatile Solids (.S) per cubic meter of reactor A relati"ely high organic

loading rate facilitated the formation of anaeronic granules in UASB systems

In general, there are two ways to design an UASB reactor.

#. &' input "$ is )*** + ,)*** mg-# or more. the design

method should be used based on "rganic #oading Rate

$. &' input "$ less than )*** mg-#. the design method should

be based on /elocity

'et/s take an example

Data

0aste water input flow rate (1) 2 345 m67day

+ 2 #5,&&& mg7' 2 #5 kg7m6

rganic loading rate 2 55 kg +7m6day (! found that organic loading rate is

sometimes state of art in wastewater treatment design Some "endors may ha"e

already had the data)

.olume of tank 2 1 x + 7'8 2 345 x #5 7 55 2 #%& m6

ote* the abo"e "olume is the actual "olume 9ou need to add more "olume (as "oid"olume)

+alculating an UASB Tan, Based on -elocit"

hen input +$/ 1#000 mg2l# using the method base on $&% is not effective in operation process

because the granular sludge will be hardl" formed. Therefore# the design criteria must be3

Upflow velocit" - 5 0#1 m2h. *"draulic retention time *&T 6 4 h +hosen in table 7# the height of

sludge is *s 8 9 1 m The height of setting area *Se 6 7.: m The volume of the UASB reactor3

8 ; x *&TThe area of the UASB reactor3 A 8 - 2 ;

&ead on http322www.slideshare.net2nitin"adav7


4/16

Slope of the separator bottom from 41 9 of reactor area.*eight of separator from 7.1 9 : m

The baffles to be installed beneath the gas domes should overlap the edge of the domes over a

distance from 70 9 :0 cm

+onstruct material3 !n the anaerobic conditions of an UASB reactor# there is a ris, of corrosion in

two main situations3

Some *:S gas can pass the ?S% separator and accumulate above the water level in the top of the

reactor. This will be oxidi@ed to sulphate b" ox"gen in the air to form Sulphuric Acid that will inturn cause corrosion of both concrete and steel. Below the water level3 +alcium $xide# (+a$)# in

concrete can be dissolve with b" +arbon /ioxide# (+$:)# in the li'uid in low p* conditions. To avoid

these problems# the material used to construct the UASB reactor should be corrosion resistant#

such as stainless steel or plastics# or be provided with proper surface coatings# (e.g. coated

concrete rather than coated steel# plastic covered with impregnated hardwood for the settler#

plastic fortified pl"wood# etc).

YOU NEED ONE TECHNICAL PERSON WITH

EXPERIENCE TO RUN A PROPER UASBR SYSTEM.

O%$'(+)- & M+-($--$ /O&M

$peration criteria3 The optimum p* range is from


5/16

An UASB reactor re'uires a long time for startup# e.g. from : 9 wee,s in good conditions (t H

:0o+) and sometimes the startup can ta,e up to 9 4 months. !n startup process# h"draulic

loading must be 5 10> of the design h"draulic loading.

The startup of the UASB reactor can be considered to be complete once a satisfactor"

performance of the s"stem has been reached at its design load.

S)'$; ((%;-%($5..+-)'*$*10710410


6/16

removed from time to time through a separate pipe and sent to a simple

sand bed for dr"ing.

D$*+- A%%')

S+>$ )2 R$()'3 ?enerall"# UASBs are considered where temperature inthe reactors will be above :0+. At e'uilibrium condition# sludge

withdrawn has to be e'ual to sludge produced dail". The sludge produced

dail" depends on the characteristics of the raw wastewater since it is the

sum total of (i) the new -SS produced as a result of B$/ removal# the

"ield coefficient being assumed as 0.7 g -SS2 g B$/ removed# (ii) the

nondegradable residue of the -SS coming in the inflow assuming 40> of

the -SS are degraded and residue is # and (iii) Ash received in the

inflow# namel" TSS-SS mg2l. Thus# at stead" state conditions#S&T8 Total sludge present in reactor# ,g Sludge withdrawn per da"#

,g2d

8 0 to 10 da"s.

Another parameter is *&T which is given b"3

*&T8 &eactor volume# m

=low rate# m 2h

8 J to 70 h or more at average flow.

The reactor volume has to be so chosen that the desired S&T value is

achieved. This is done b" solving for *&T from S&T e'uation assuming (i)

depth of reactor (ii) the effective depth of the sludge blan,et# and (iii) the

average concentration of sludge in the blan,et (0 ,g2m). The full depth

of the reactor for treating low B$/ municipal sewage is often 4.1 to 1.0 m

of which the sludge blan,et itself ma" be :.0 to :.1 m depth. =or high

B$/ wastes# the depth of both the sludge blan,et and the reactor ma"

have to be increased so that the organic loading on solids ma" be ,ept

within the prescribed range.

$nce the si@e of the reactor is fixed# the upflow velocit" can be

determined from

Upflow velocit" m2h 8 &eactor height

*&T# h

Using average flow rate one gets the average *&T while the pea, flow

rate gives the minimum *&T at which minimum exposure to treatment

occurs. !n order to retain an" flocculent sludge in reactor at all times#experience has shown that the upflow velocit" should not be more than


7/16

0.1 m2h at average flow and not more than 7.: m2h at pea, flow. At

higher velocities# carr" over of solids might occur and effluent 'ualit" ma"

be deteriorated. The feed inlet s"stem is next designed so that the

re'uired length and width of the UASB reactor are determined.The settling compartment is formed b" the sloping hoods for gas

collection. The depth of the compartment is :.0 to :.1 m and the surface

overflow rate ,ept at :0 to :J m 2m:da" (7 to 7.: m2h) at pea, flow. The

flow velocit" through the aperture connecting the reaction @one with the

settling compartment is limited to not more than 1 m2h at pea, flow. /ue

attention has to be paid to the geometr" of the unit and to its h"draulics

to ensure proper wor,ing of the L?as%i'uidSolidSeparator (?%SS)L the

gas collection hood# the incoming flow distribution to get spatialuniformit" and the outflowing effluent.

P=*+5 P'$($'*

A single module can handle 70 to 71 M%/ of sewage. =or large flows a

number of modules could be provided. Some ph"sical details of a t"pical

UASB reactor module are given below3

Reactorconfiguration

Rectangular or circular. Rectangular shape is preferred

Depth 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.

ength !s necessar".

#nlet feed

gra$it" feed from top %preferred for municipal sewage& or pumped feed from

bottom through manifold and laterals %preferred in case of soluble industrial

wastewaters&.

'ludge blan(et

depth2 to 2.5 m for sewage. )ore depth is needed for stronger wastes.

Deflector*+''

This is a deflector beam which together with the gas hood %slope ,0& forms a

gas-liuid-solid-separator %+''& letting the gas go to the gas collection

channel at top/ while the liuid rises into the settler compartment and the

sludge solids fall bac( into the sludge compartment. The flow $elocit" through

the aperture connecting the reaction one with the settling compartmentt is

generall" limited to about 5m*h at pea( flow.

'ettler

compartment2.0-2.5 m in depth. 'urface o$erflow rate euals 20-2 m*m2*d at pea( flow.

P')$** D$*+- P'$($'*


8/16

A few process design parameters for UASBs are listed below for municipal sewages with

B$/ about :0000 mg2l and temperatures above :0+.

3RT -10 hours at a$erage flow %minimum 4 hours at pea( flow&'RT 0-50 da"s or more

'ludge blan(et concentration

%a$erage&15-0 (g '' per m. !bout 0 (g T'' per m.

6rganic loading on sludge

blan(et

0.-1.0 (g 76D*(g '' da" %e$en upto 10 (g 76D* (g '' da"

for agro-industrial wastes&.

olumetric organic loading1- (g 76D*m da" for domestic sewage %10-15 (g 76D*m da"

for agro-industrial wastes&

86D*76D remo$al efficienc" 'ewage 5-59 for 86D. 4-9 for 76D.

#nlet points )inimum 1 point per .-4.0 m2 floor area.

:low regime ;ither constant rate for pumped inflows or t"picall" fluctuatingflows for gra$it" s"stems.


9/16

UASB

B$/ 700 ppm 40 ppm J0>

+$/ 00 ppm 7:0 ppm

TSS 7J00 ppm 410 ppm 1>

FLOW IN UAS# ? 1700 KLD /T@+- 255 2('$ %+(= +-()

)-(

!nfluent +$/ 00 ppm 8 4N10 Eg

Gffluent +$/ 8 7NJ0 Eg

+$/ removed in a da" 8 :N0 ,g

Bi! g&s #'!+*)e+ @ 4. )* 5-' #e' g !" COD 'e5!6e+ 7 /89 )* 5-' #e' +&.

C&)i- !" g&s ;!$+e':

T;e #'i5&' #*'#!se !" & g&s ;!$+e' is -! &+


10/16

ENVO PRO=ECT>S FIRST UASBR PRO=ECT WAS IN /442. SOME OF OUR

PRO=ECT PHOTOS


11/16

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12/16

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