Flow Properties of Animal Waste Slurries
`
`M. Kumar, H. D. Bartlett, N. IM. Mohsenin
`M E M B ER
`M E M B ER
`ASAE
`ASAE
`
`AGRICULTURAL production and
`
`processing generates much organic
`waste which is of significant economic
`and aesthetic impact. Livestock manure
`and associated waste water from large
`scale animal production systems, crop
`residues and waste
`from processing
`plants constitute the principal source of
`waste.
`Hydraulic transport provides a clean
`and low cost method of handling these
`waste materials as a slurry. However,
`little data are available on the flow
`properties of such organic waste mater(cid:173)
`ials for design of hydraulic
`transport
`systems.
`This paper reports on work done to
`develop a coaxial cylinder viscometer
`for determining the shear diagrams and
`viscosities of animal waste slurries with
`respect to dilution, sawdust content and
`temperature (Kumar, 1969). The effect
`of Dilution on the flow properties was
`determined in order to establish opti(cid:173)
`mum consistency
`for pumping effi(cid:173)
`ciency. Because sawdust is a commonly
`used bedding material, its effect on flow
`properties was included in this investiga(cid:173)
`tion. The study of flow properties of
`manure slurries in relation to tempera(cid:173)
`tures was included because of the vary(cid:173)
`ing temperatures under which the ma(cid:173)
`terial is handled.
`
`RELATED RESEARCH
`Extensive research has been done on
`the biological decomposition of excre(cid:173)
`ment, but very little has been reported
`on the flow properties of these fluids.
`Taiganides et al, (1964) stated there is a
`lack of basic information on the physi(cid:173)
`cal and chemical properties of manure,
`which are needed for
`the design of
`handling
`and
`treatment
`equipment.
`Hansen (1959) in studying manure han(cid:173)
`dling systems, indicates that a difficulty
`involved in the design of liquid manure
`
`Article was submitted for publication on
`November 9, 1970; reviewed and approved
`for publication by the Structures and En(cid:173)
`vironmental Division of ASAE on December
`28, 1971.
`Authorized for publication as paper num(cid:173)
`ber 3874 in the Journal Series of the Penn(cid:173)
`sylvania Agricultural Experiment Station.
`The authors are: M. KUMAR, Graduate
`Assistant, H. D. BARTLETT
`and N. N.
`MOHSENIN, Professors, Agricultural Engi(cid:173)
`neering Dept., Pennsylvania State University,
`University Park.
`
`718
`
`pumps is the complexity of the physical
`and chemical nature of the material.
`According to Schneider (1958), manure
`being a mixture of solids and water
`should be treated as non
`free-flowing
`materials with non-Newtonian
`flow
`characteristics. Sobel (1965) described
`the flowability of manure and classified
`it into three categories, semisolid, semi-
`liquid and liquid.
`Hart et al. (1966) indicates that a
`slurry of between one and four percent
`total solids content is a good compro(cid:173)
`mise between excessive volume and easy
`handling.
`In studying the flow properties of
`disperse systems, Herman (1953) ob(cid:173)
`served that the presence of rigid parti(cid:173)
`cles in a flowing solvent disturbed the
`initial flow and that the energy dissi(cid:173)
`pated inside the flowing mass was in(cid:173)
`creased. Stepanoff
`(1964) states
`that
`solids suspended
`in a liquid cannot
`absorb, store or transmit pressure en(cid:173)
`ergy which is a property of fluids. Estep
`(reference 7) suggests that a manure
`pump installation might well be designed
`for friction head loss 10 percent greater
`than would be expected for water.
`Mohsenin
`(1970) defines
`a non-
`Newtonian fluid as a fluid in which the
`relationship between shear stresses and
`shear rates is nonlinear. Apparent visco(cid:173)
`sity as applied to non-Newtonian fluid is
`the viscosity of a Newtonian
`liquid
`exhibiting the same resistance to flow at
`the chosen shearing stress or shearing
`rate. It is determined from the slope of
`a straight line connecting the chosen
`points on the nonlinear curve to the
`origin.
`Herman (1953) found that in many
`cases, even
`in very dilute solutions,
`there was no constant viscosity coeffi(cid:173)
`cient
`and,
`accordingly, Newtonian
`methods of analysis could not be ap(cid:173)
`plied
`to
`the solutions. Mitchell and
`Peart (1968), Van Gilst et al. (1966),
`and Herum et al. (1966) individually
`conducted a study on
`the apparent
`viscosity of several organic slurries con(cid:173)
`sisting of ground corn and water which
`had a moisture content range from 63.6
`percent
`to 75 percent wet basis. The
`slurries studied showed
`time depen(cid:173)
`dency effects.
`Charm (1963 and 1960) and Harper
`and Elsahrige
`(1965) have
`reported
`
`some data on flow constants for several
`organic fluids and food materials.
`Steiner (1960) showed that melted
`chocolate follows Casson's equation:
`
`[ i]
`
`However, Harper (1961), who employed
`a specially designed concentric cylinder
`viscometer for obtaining shear stress and
`shear rate on pear puree and tomato
`concentrates, stated that Casson's equa(cid:173)
`tion was more difficult to use and did
`not give good agreement with experi(cid:173)
`mental data as a power law equation.
`According
`to Caldwell and Babbitt
`(1941) a standard viscometer may be
`designed and calibrated so that pipe
`flow can be evaluated by this visco(cid:173)
`meter.
`
`THEORETICAL CONSIDERATION
`According
`to Van Wazer et al.
`(1963), when a rotating body is im(cid:173)
`mersed in a liquid it undergoes a viscous
`drag, which is a function of the speed of
`rotation of
`the body. In using
`the
`viscosity equation, the relationship be(cid:173)
`tween the rate of shear and the shearing
`stress is the same, whether the bob or
`the cup is rotated. The chief advantage
`of rotational viscometric procedures is
`that continuous measurements, at a
`given rate of shear or shear stress, may
`be made for extended periods of time.
`Subsequently, measurements such as
`time-dependency may be determined.
`A comprehensive description of rota(cid:173)
`tional viscometer designs is given by
`Wilkinson (1960). The most common
`type
`is
`the coaxial cylinder device,
`which consists of a cylinder (bob) of
`radius Rb suspended in the sample fluid
`in a cup of radius Rc. The liquid covers
`the inner cylinder to a height h. The
`bottom of the inner cylinder is separ(cid:173)
`ated from the bottom of the cup by a
`distance #. The cup rotates with an
`angular velocity ^.
`The following assumptions are made
`(Eirich, 1960):
`1. The liquid is incompressible.
`2. The motion of the liquid is not
`turbulent.
`3. The stream lines are circles on
`the horizontal plane perpendicular
`to
`the axis of rotation.
`
`TRANSACTIONS of the ASAE - 1972
`
`Exhibit 1129
`Bazooka v. Nuhn - IPR2024-00098
`Page 1 of 5
`
`

`

`PULLEYv
`
`FRAME>
`
`STEM-
`
`VENTS
`
`-BOB (20. 40 cm dia )
`
`WEIGHT
`
`TEMP
`CONTROL
`BATH
`
`DRAIN
`
`l _n^ - C U P ( 2 6 cm dia)
`
`ANNULAR GAP (2.80cm)
`
`TELECOUNTER
`
`BOTTOM CLEARANCE (2.7 cm)
`
`'VARIABLE SPEED DRIVE
`FIG. 1 Schematic diagram of coaxial cylinder viscometer.
`
`4. The motion of the fluid in the
`bob is stationary.
`5. There is no relative motion be(cid:173)
`tween the cylinders and the material in
`immediate contact with the cylinder.
`6. The motion of the liquid is the
`same on each plane perpendicular to the
`axis of rotation, that is, the motion is
`incompressible,
`i.e. neglect
`the edge
`effect, end effect and normal forces
`(cross viscosity, Weissenberg
`effect,
`etc.).
`the
`the steady state of flow,
`In
`external
`torque equals
`the opposing
`torque in the fluid, such that:
`
`n
`
`2
`
`Tco
`
`c
`
`1;
`
`n M
`
`/ b_\ 2 / ni
`R
`
`[5]
`
`Taking the logarithm of both sides,
`equation [5] can be converted to the
`slope-intercept form of the equation of
`a straight line, with log Too versus log £2.
`The slope of this line is the exponent n.
`With the value of the exponent known,
`the constant c can be calculated from
`equation [ 5 ].
`Apparent viscosity can be deter(cid:173)
`mined as:
`
`M
`
`27rr2 hT
`
`[21
`
`V" = c1,n T C o( 1-1 / n)
`
`. . ..
`
`[6]
`
`Non-Newtonian flow is the general
`case where the rheological behavior can
`be shown with power law equations.
`The equation for each special case can
`be derived from the equations of non-
`Newtonian flow by using the correct
`value of exponent n.
`The empirical power law equation is
`as follows:
`
`T
`
`dco
`c(-r —
`dr
`
`)"
`
`Th e moment is:
`
`dCO
`0
`r,
`M = 2TT r h T = 27T r2 h c (-r
`dr
`
`[3]
`
`f
`
`[ 4]
`
`t he
`for
`integrating
`and
`Rearranging
`b o u n d a ry values and substituting for M
`in terms of shear stress, Tco, at t he inner
`cylinder, it can be reduced t o:
`
`1972 - TRANSACTIONS of the ASAE
`
`End Effect
`The previous assumptions are valid
`infinitely
`long cylinders. There
`is
`for
`always a viscous drag due to t he stress
`on t he b o t t om surface of the b ob and
`the cup.
`to Lindsley a nd Fisher
`According
`( 1 9 4 7 ),
`there are four ways of deter(cid:173)
`mining t he end effect. The m e t h od used
`in this paper is to calibrate the
`instru(cid:173)
`ment with
`liquids of k n o wn viscosity,
`thus, absorbing
`the end effect
`in
`t he
`i n s t r u m e nt constant.
`E nd effect m ay be considered as
`equivalent to an increase in t he effective
`depth of immersion from h to h + Ah.
`Therefore, in t he r o t a t i o n al coaxial cy(cid:173)
`linder viscometer
`
`477 (h+Ah)
`
`M
`
`7? £2
`
`[7]
`
`K
`
`Rz
`
`FIG. 2 The coaxial cylinder viscometer.
`
`where Ah is the end correction and it is
`a function of Rb, R , h and £•
`M
`i
`^
`i
`•
`i
`——
`By
`p l o t t i ng
`the graph
`versus h and extending the straight line
`towards axis h, it will give the intercept
`on the x-axis, which will be equal to Ah.
`For separation at the bottom greater
`than 1 cm and for viscosity within the
`range of 1 to 150 poise, the end effect is
`nearly constant. Calibration of the ap(cid:173)
`paratus with a single standard sample is
`sufficiently accurate for most purposes.
`
`INVESTIGATION PROCEDURE
`A viscometer was designed after con(cid:173)
`sidering the desirable features of
`the
`coaxial cylinder viscometer, which were
`given by Harper (1961). The turbulent
`flow criteria, Merril (1956), as given
`below, was incorporated in the design:
`
`2TT RK (R - RJ N C
`
`< 500
`
`. .
`
`[8]
`
`C = density of fluid
`N = revolutions of rotor per second
`The basic components of coaxial
`cylinder viscometer are shown sche(cid:173)
`matically in Fig. 1 and illustrated in Fig.
`2.
`
`electrically powered variable
`An
`speed hydraulic drive was coupled
`through a train of pulleys and V-belts to
`rotate the cup. The cup was made of
`steel 26 cm inside diameter and 35.50
`cm long. An annular gap was provided
`to
`fill with hot or cold
`liquid
`for
`maintaing a constant temperature.
`Two drain valves were provided for
`removing the sample material and con(cid:173)
`stant temperature liquid.
`The other component of the coaxial
`head consisted of an aluminum cylinder
`(bob) 20.40 cm outside diameter by
`30.50 cm long. The cylinder was open
`at the bottom and had four vent holes
`of 1.25 cm diameter at the top.
`A frame structure with four corner
`members and two cross members was
`used
`to support
`the bob; slots were
`made in the crosshead member to pro-
`
`7 19
`
`Exhibit 1129
`Bazooka v. Nuhn - IPR2024-00098
`Page 2 of 5
`
`

`

`TABLE 1. PARTICLE SIZE AND DISTRIBUTION
`OF FRESH MANURE
`
`Particle size,
`mm
`
`Total solids
`retained on
`sieve, g
`
`Percentage
`of
`total solids
`
`Percentage
`by weight
`
`4.669
`2.380
`1.190
`0.595
`0.297
`0.105
`0.119
`
`1.0548
`2.6032
`1.9933
`1.4131
`1.5513
`0.9512
`0.6432
`
`5.2870
`
`6.808
`16.798
`12.862
`9.118
`10.010
`6.138
`4.138
`
`34.116
`
`93.192
`76.394
`63.532
`54.414
`44.404
`38.266
`34.116
`
`Sieve
`
`4
`8
`16
`30
`50
`100
`1 40
`Finer than
`1 40
`
`three viscometers,
`was measured by
`n a m e l y; C a p i l l a r y,
`Stormer
`and
`MacMichael.
`The mean viscosity of the SAE-90
`oil, at 70 F was determined as 347.10
`centipoise. The viscosity of the above
`oil measured by the coaxial cylinder
`viscometer was found as 414.21 centi(cid:173)
`poise.
`
`vide a means for positioning the bob
`coaxially with the cup. The bob was
`supported by a vertical shaft referred to
`as
`the stem.
`It was supported and
`aligned in the crosshead frame member
`with
`two antifriction
`tapered
`roller
`bearings.
`A telecounter was mounted on the
`frame
`for measuring
`the number of
`revolutions.
`A torque pulley of 13 cm diameter
`was mounted on the top of the stem.
`An antifriction pulley was mounted
`the frame structure to support a
`to
`restraining cord. One end of the cord
`was connected to the periphery of the
`pulley and the other end supported the
`hanging weight which could be adjusted.
`The coaxial cylinder viscometer was
`adjusted for uniform annular gap and
`clearance between the bottom of the
`bob and cup.
`fluid
`The viscosity of an organic
`depends on its physical and chemical
`properties, moisture
`content,
`total
`solids, volatile solids, fixed solids, par(cid:173)
`ticle density, bulk density and particle
`sizes and distribution. These properties
`were determined according to ASTM
`(1968) specifications.
`The chemical properties, such as
`crude protein, crude fiber, ether extract,
`nitrogen
`free extract and ash, were
`determined by the standard procedure
`(Triebold and Aurand, 1963) which had
`been modified at The Pennsylvania State
`University.
`
`DETERMINATION OF
`APPARATUS CONSTANT
`Apparatus constant is a factor which
`gives the true apparent viscosity after
`multiplying it by the theoretical veloc(cid:173)
`ity. This method has the advantage of
`including all of the end and edge effects,
`slippage,
`turbulent
`interferences, etc.
`and
`allows calculation of apparent
`viscosity directly
`from
`the measured
`data.
`The apparatus constant was obtained
`by calibration of the viscometer with a
`standard fluid (oil-SAE-90). Its viscosity
`
`720
`
`.". Apparatus Constant =
`
`347.10
`
`= 0.8380
`
`414.21
`MATERIALS FOR ANALYSIS
`Samples of fresh manure were ob(cid:173)
`tained directly as excreted from lac-
`tating Brown Swiss cows, on a ration of
`grain, hay and silage, at the dairy center
`of
`the Pennsylvania State University.
`Also, samples were obtained from the
`gutter which contained urine, bedding,
`grit and waste forage. In addition, sam(cid:173)
`ples were taken from the liquid manure
`storage tank which contained bedding,
`urine, fresh and old manure and water.
`
`TESTING PROCEDURE
`Quantities of the respective samples
`were poured into the cup to a height of
`20 cm on the bob. The viscometer was
`turned on to a preselected speed setting
`and weight was added to the torque
`measuring cord until the bob remained
`in a fixed position, denoting that the
`torque due to the product of the ap(cid:173)
`plied weight times the radius of the
`torque pulley was equal to the torque
`due to shearing force in the slurry. The
`time for 20 revolutions was measured
`with a stopwatch. The rotational speed
`was then changed to another setting and
`the weight was adjusted for equilibrium
`conditions. The procedure was repeated
`for a minimum of six settings. The
`temperature was maintained constant
`by filling the outer gap with hot or cold
`water or ice, which was required to have
`the same temperature for each sample.
`In this manner shear stress and shear
`rate were determined and shear dia(cid:173)
`grams were plotted.
`
`For determining the effect of dilu(cid:173)
`tion on viscosity, five dilutions were
`used. The different dilutions were made
`by adding water to the manure. All
`values of solids content were deter(cid:173)
`mined on a dry basis. Three levels of
`sawdust content (0, 5 and 10 percent)
`were used to determine the effect of
`sawdust on the viscosity of manure.
`Three temperatures (46, 76 and 108
`F) were utilized to evaluate the effect of
`temperature on the viscosity of the
`manure. The samples were cooled to 46
`F in a cold room prior to running the
`test. To attain the 108 F temperature,
`the samples were heated on a hot plate.
`The temperature was maintained con(cid:173)
`stant for all of these tests by adding
`cold or hot water or ice to the annular
`gap which worked as a constant tem(cid:173)
`perature bath.
`In addition, tests were run at 76 F on
`samples of manure from the gutter and
`from the liquid manure storage pit.
`
`RESULTS DETERMINED
`Physical characteristics and chemical
`properties of fresh cow manure:
`Moisture content - 84.52 percent
`Total solids content = 15.48 per(cid:173)
`cent
`Volatile solids (on the basis of
`total solids content) = 89.43 per(cid:173)
`cent
`Fixed solids (on the basis of total
`solids content) = 10.57 percent
`Bulk density
`(at 84.52 percent
`moisture content) = 1.12 g per cc
`Average particle density = 1.43 g
`per cc
`Crude Protein = 13.73 percent
`Crude Fiber = 27.36 percent
`Ash = 10.57 percent
`Ether Extract = 5.70 percent
`Nitrogen Free Extract = 42.64
`percent Particle size and distribu(cid:173)
`tion was as shown in Table 1.
`
`Effect of Dilution
`As total solids content was decreased
`at constant
`shear
`rate, shear stress,
`viscosity index and apparent viscosity
`were decreased, see Table 2 and Fig. 3.
`When the slurry was below five percent
`total solids content, it showed Newton(cid:173)
`ian flow properties, and above six per(cid:173)
`cent it showed non-Newtonian (pseudo-
`plastic) flow properties.
`
`Effect of Sawdust
`All mixtures of sawdust and manure
`above six percent total solids content
`s h o w ed
`a
`p s e u d o p l a s t ic
`( n o n-
`Newtonian) behavior. However,
`the
`flow at five percent sawdust level and
`
`TRANSACTIONS of the ASAE - 1972
`
`Exhibit 1129
`Bazooka v. Nuhn - IPR2024-00098
`Page 3 of 5
`
`

`

`TABLE 2. CONSOLIDATION OF RESULTS FROM VARIABLE
`SHEAR STRESS TESTS
`Total
`solids
`content,
`percent
`11.02
`9.28
`8.59
`7.69
`6.17
`11.11
`8.85
`7.78
`5.30
`10.91
`9.08
`7.96
`6.06
`8.60
`7.03
`5.15
`4.08
`8.60
`7.03
`5.15
`4.08
`14.82
`10.95
`7.22
`6.47
`11.05
`8.45
`
`Description
`
`Fresh manure with
`no sawdust
`
`Fresh manure with
`5 percent sawdust
`
`Fresh manure with 10
`percent sawdust
`
`Fresh manure
`
`Fresh manure
`
`Manure from gutter
`
`Manure from liquid
`storage pit
`
`Temp.,
`deg F
`
`76
`"
`"
`"
`"
`76
`
`j»
`
`" >5
`
`76
`>»
`"
`>>
`46
`" >5
`"
`1 08
`"
`»»
`"
`76
`"
`»»
`"
`76
`»
`
`Shear stress,*
`dynes per sq
`cm
`715.0
`444.0
`353.5
`230.0
`64.0
`1000.0
`296.0
`105.0
`22.0
`633.5
`207.0
`91.2
`28.0
`589.0
`434.3
`140.3
`42.3
`302.0
`285.0
`45.0
`12.2
`815.0
`291.8
`82.1
`73.6
`300.0
`120.0
`
`n
`
`0.3820
`0.2980
`0.2745
`0.3645
`0.5428
`0.4326
`0.3705
`1.4590
`1.000
`0.4698
`0.3549
`0.5000
`0.6411
`0.3220
`0.2863
`1.0000
`1.0000
`0.2610
`0.3800
`1.0000
`1.0000
`0.3783
`0.6026
`0.6945
`0.5963
`0.6094
`0.8391
`
`c
`dynes-sec11
`cm
`
`195.000
`160.251
`137.298
`66.854
`12.619
`229.3239
`83.822
`22.163
`0.734
`128.062
`61.490
`16.383
`2.939
`198.320
`162.748
`4.746
`1.412
`125.381
`65.011
`2.177
`0.601
`225.429
`37.2204
`7.824
`9.698
`37.223
`6.818
`
`Apparent*
`viscosity,
`centipoise
`
`1997.10
`1217.45
`944.86
`649.86
`268.46
`3328.00
`823.44
`296.91
`61.51
`1766.33
`567.31
`246.62
`69.73
`1679.56
`1180.66
`397.71
`118.33
`871.99
`669.39
`182.43
`50.36
`2285.55
`802.15
`233.12
`206.12
`818.74
`329.66
`
`2 8 00
`
`_
`
`2 4 00
`
`2 0 00
`
`1500
`
`1200
`
`8 00
`
`-
`
`4 00
`
`0
`5.3
`
`—
`
`- 0 % SAWDUST
`-
`5 % SAWDUST
`
`/
`/
`
`/
`1
`'
`
`/
`
`//
`
`•'
`/
`
`^'
`
`/
`
`/
`
`/
`
`/
`
`./
`
`^'
`
`6
`
`7
`
`8
`
`9
`
`10
`
`II
`
`- "
`
`5
`
`ntif ^
`
` > (-
`
`VISC0S
`
`APPARENT
`
`TOTAL SOLIDS CONTENT
`(•%)
`FIG. 5 Apparent viscosity of fresh manure at
`76 F for various total solids content and
`sawdust levels (shear rate 30 2 per sec).
`
`Effect of Temperature
`Experiments were run at 46, 76 and
`108 F to determine the effect of tem(cid:173)
`perature on viscosity of manure. Below
`5.15 percent total solids content at 76 F
`and 108 F the flow was Newtonian, and
`above 6.17 percent at 46, 76 and 108 F,
`pseudoplastic
`(non-Newtonian)
`flow
`was observed. The exact transition point
`between Newtonian and non-Newtonian
`flow was difficult to establish.
`Shear diagrams and graphs of appar(cid:173)
`ent viscosity versus total solids content
`at different temperatures are shown in
`Fig. 6 and Fig. 7, respectively. It can be
`seen
`from
`the graphs
`that apparent
`viscosity of manure increases with a
`decrease in temperature in the range of
`46 F to 76 F. At 108 F the apparent
`viscosity was greater than at 76 F and
`the slope of the curve also changed. It
`would appear that, at the higher temper(cid:173)
`ature,
`some chemical changes
`took
`place, causing a change in the physical
`and chemical properties of the slurry. A
`similar type of occurrence was obtained
`by Herum et al. (1966) when working
`with swine feed.
`
`Manure from Gutter
`These
`samples contained digested
`material as well as urine, sawdust, grit
`
`* Shear stresses and apparent viscosities are calculated at shear rate of 30 1 per sec.
`
`total solids content was
`5.3 percent
`found to be Newtonian. Apparent vis(cid:173)
`cosity of manure without sawdust, up
`to approximately nine percent
`total
`solids content, was more than the five
`and. ten percent sawdust mixtures. This
`was believed to be due to a decrease of
`cohesive forces between manure parti(cid:173)
`cles. At this dilution, there was enough
`water to give good slippage of manure
`particles. Therefore, shearing force was
`decreased and
`the apparent viscosity
`was less. Above nine percent total solids
`content (five percent sawdust) apparent
`viscosity increased over the values for
`manure without sawdust. Apparently
`the frictional
`forces due to sawdust
`particles
`increased and
`the cohesive
`forces between manure particles re(cid:173)
`mained the same, causing an increase in
`
`apparent viscosity. Above approximate(cid:173)
`ly 11.2 percent total solids content (10
`percent sawdust) the apparent viscosity
`was greater than with no sawdust. In
`this case there was insufficient water to
`separate the individual particles. There(cid:173)
`fore,
`the measurements indicated
`the
`frictional forces between individual saw(cid:173)
`dust particles, instead of the slippage of
`the fluid. This effect is shown in Fig. 4
`and Fig. 5.
`
`/ ^^ 10% (10.91 )
`
`E 6 00
`
`0 % ( 9 . 2 8)
`
`<
`
`3 00
`
`0 % ( 8 . 5 9)
`
`5% ( 8 . 8 5)
`
`0 % ( 7 . 6 9)
`
`1 0% ( 9 . 0 8)
`
`5% ( 7 . 7 8)
`_
`^ V i/ 1 0% ( 7 . 9 6)
`^ ^ ^ • ^ • ^ 0%
`(6.17)
`
`r^
`
`5% ( 5 . 3 0)
`
`20
`
`40
`30
`SHEAR RATE
`
`50
`( I / s ec )
`
`60
`
`70
`
`FIG. 3 Shear diagram (effect of dilution on
`fresh manure at 76 F).
`
`0
`
`10 20 30 40 50 60 70 80 90
`SHEAR RATE ( l / s ec )
`FIG. 4 Shear diagram
`(effect of sawdust
`content, percent, on fresh manure at 76 F).
`
`SHEAR RATE (
`FIG. 6 Shear diagram (effect of temperature
`and dilution effect on fresh manure.
`
`1972 - TRANSACTIONS of the ASAE
`
`721
`
`Exhibit 1129
`Bazooka v. Nuhn - IPR2024-00098
`Page 4 of 5
`
`

`

`<D 2000|
`
`2
`
`10
`8
`6
`4
`TOTAL SOLIDS CONTENT ( %)
`
`12
`
`FIG. 7 Apparent viscosity of fresh manure at
`various total solids content and temperature
`(shear rate 30 £ per sec).
`
`and waste forage. The results of tests on
`manure from the gutter at various dilu(cid:173)
`tions are given in Table 2.
`
`VISCOSITY OF LIQUID MANURE
`FROM MANURE STORAGE TANK
`Samples were obtained
`from
`the
`liquid manure storage tank and analyzed
`for forage straw, manure particles, saw(cid:173)
`dust, crude fibre, grit particle and mois(cid:173)
`ture content. The original sample of
`liquid manure was found to have 11.05
`percent total solids. It's apparent viscos(cid:173)
`ity was 818.74 centipoise at 76 F. After
`diluting to 8.45 percent the apparent
`viscosity was reduced to 329.66 centi(cid:173)
`poise. The
`flow
`in both cases was
`pseudoplastic (non-Newtonian). The re(cid:173)
`sults are tabulated in Table 2.
`
`CONCLUSIONS
`
`It was found that the coaxial cylin(cid:173)
`der type viscometer is suitable for rheo-
`metry of organic waste slurries. The
`time dependency study of the slurries
`can be investigated by this viscometer.
`The viscosity of manure slurry decreases
`with an
`increase
`in dilution. It was
`further
`noticed
`that
`the
`flow
`is
`Newtonian at low total solids content
`
`(below five percent). The addition, of
`sawdust up to as much as 10 percent by
`weight of the amount of manure de(cid:173)
`creases the viscosity of a slurry having a
`total solids contents up to approximate(cid:173)
`ly nine percent. Furthermore,
`it was
`noted that the viscosity of fresh manure
`slurry decreases with an
`increase of
`temperature.
`
`References
`11
`Part
`S t a n d a r d s,
`1 A S TM
`Bituminous materials for highway construc(cid:173)
`tion, waterproofing and roofing; soils, skid
`resistance. 1968. American Society for Test(cid:173)
`ing and Materials, Philadelphia.
`2 Caldwell, A. and E. Babbitt. 1941.
`The flow of muds, sludges and suspensions in
`circular
`p i p e. T r a n s, of
`the AICE
`37(l):237-266.
`3
`Casson, N. 1959. Rheology of dis(cid:173)
`perse systems. (C. C. Mill edition) Pergamon
`Press, New York.
`4
`Charm, S. E. 1963. The direct deter(cid:173)
`mination of shear stress-shear rate behavior of
`feeds in the pressure of a yield stress. Journal
`of Food Science 28(1): 107-113.
`5
`Charm, S. E. 1960. Viscometry of
`non-Newtonian
`food materials. Food Re(cid:173)
`search 25(1): 351-362,
`6
`Eirich, F. R. 1960. Rheology, theory
`and applications Vol. 3. Academic Press, New
`York and London, 29, 30, 31, 37.
`7
`Estep, A. J. Handling liquid manure
`by sprinklers. Unpublished paper, Cooperative
`Extension Service, Washington State Univer(cid:173)
`sity, Vancouver, Washington.
`8 Hansen, C. M. 1959. Engineering
`principles in handling liquid materials. AGRI(cid:173)
`CULTURAL ENGINEERING 39(9):546-551.
`9 Harper, J. C. 1961. Coaxial cylinder
`viscometry for non-Newtonian
`fluids. The
`R e v i ew
`of
`Scientific
`I n s t r u m e n ts
`32(4):425-428.
`10 Harper, J. C. and A. F. Elsahrige.
`1965. Viscometric behavior of tomato con(cid:173)
`c e n t r a t e s.
`J o u r n al
`of Food Science
`30(3):470-476.
`11 Hart, S. A., J. A. Moore and W. H.
`Hale. 1966. Pumping manure slurries. Pro(cid:173)
`ceedings of National Symposium on Animal
`Waste Management. ASAE Publication No.
`SP-0366, 34, American Society of Agricultur(cid:173)
`al Engineers, St. Joseph, Mich. 49085.
`12 Herman, J. J. 1953. Flow properties
`of disperse systems. Interscience Publishers,
`Inc. New York.
`13 Herum, F. L., G. W. Issacs and R. M.
`Peart. 1966. Flow properties of the highly
`viscous organic pastes and slurries. TRANS(cid:173)
`ACTIONS OF THE ASAE 9(l):45-47, 51.
`14 Kumar, M., 1969. Flow properties of
`animal waste slurries. M. S. Thesis, Agricultur(cid:173)
`al Engineering Department, The Pennsylvania
`State University, University Park, Pa.
`15
`Lindsley, C. H. and E. K. Fisher.
`1947. End effect in rotational viscometer.
`Journal of Applied Physics 18(11):988-996.
`16 Merril, E. W. 1956. A coaxial cylin(cid:173)
`der viscometer
`for non-newtonian
`fluids.
`
`Instrument Society of America
`Journal
`3(4):124-128.
`17 Mitchell, B. W. and R. M. Peart.
`1968. Measuring apparent viscosity of organic
`slurries. TRANSACTIONS OF THE ASAE
`ll(4):523-525.
`18 Mohsenin, N. N. 1970. Physical
`properties of plant and animal materials. Vol.
`I: Structure, physical characteristics and me(cid:173)
`chanical properties. Gordon and Breach Sci(cid:173)
`ence Publishers, New York.
`19
`Schneider, E. C. 1958. Non-free
`flowing materials: Handling techniques for
`hay and manure. AGRICULTURAL ENGI(cid:173)
`NEERING 39(9): 558-559.
`20
`Sobel, A. T. 1965. Some physical
`properties of animal manures associated with
`handling. ASAE Paper No. NA 65-11.
`21
`Steiner, E. H. 1960. The rheology of
`disperse systems. Pergamon Press, New York.
`22
`Stepanoff, A. J. 1964. Pumping
`solid-liquid mixtures. Mechanical Engineering
`86(9):29-35.
`23
`Taiganides, E. P., E. T. Hagen, E. R.
`Baumann and H. P. Johnson. 1964. Properties
`and pumping characteristics of hog wastes.
`T R A N S A C T I O NS OF THE ASAE
`7(2):124-127,129.
`24
`Triebold, H. O. and L. W. Aurand.
`1963. Food composition and analysis, D. Van
`Nostrand Company, Inc., New York.
`25 Van Gilst, C, R. M. Peart, T. W.
`Perry and R. A. Pickett. 1966. An automatic
`slurry feeding system for swine. AGRICUL(cid:173)
`TURAL ENGINEERING 47(1):24-25,31.
`26 Van Wazer, J. R., J. W. Lyons, K. Y.
`Kim and R. E. Colwell. 1963. Viscosity and
`flow measurement. Interscience Publishers,
`Inc., New York.
`27 Wilkinson, W. L. 1960. Non-
`newtonian fluids. Pergamon Press, New York.
`
`List of Symbols
`= radius of bob, cm
`Rb
`= radius of cup, cm
`Rc
`= height of the fluid, cm
`h
`= torque on bob, dynes cm
`M
`= angular velocity of the cup, rad per
`sec
`= angular velocity of the cup, 1 1 per
`sec
`= shear stress, dynes per sq cm
`= shear stress at angular velocity u),
`dynes per sq cm
`= bottom clearance between cup and
`bob, cm
`= flow behavior index
`dynes-sec
`«
`cm
`
`T
`TCJ
`
`C
`1?
`
`1?"
`dy_
`dr
`r
`K
`Ty
`
`= viscosity index,
`
`= density of fluid
`= viscosity of fluid centipoise
`= apparent viscosity of fluid centipoise
`
`= shear rate, 1 per sec
`= radius from the axis of rotation
`= constant
`= intercept on the shear stress axis
`
`722
`
`TRANSACTIONS of the ASAE - 1972
`
`Exhibit 1129
`Bazooka v. Nuhn - IPR2024-00098
`Page 5 of 5
`
`