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Apparent viscosity
Apparent viscosity
Apparent viscosity
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The apparent viscosity of a fluid depends on the shear rate at which it is measured. The apparent viscosity of a dilatant fluid is higher when measured at a higher shear rate (η4 is higher than η3), while the apparent viscosity of a Bingham plastic is lower (η2 is lower than η1).

In fluid mechanics, apparent viscosity (sometimes denoted η)[1] is the shear stress applied to a fluid divided by the shear rate:

For a Newtonian fluid, the apparent viscosity is constant, and equal to the Newtonian viscosity of the fluid, but for non-Newtonian fluids, the apparent viscosity depends on the shear rate. Apparent viscosity has the SI derived unit Pa·s (Pascal-second), but the centipoise is frequently used in practice: (1 mPa·s = 1 cP).

Application

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A single viscosity measurement at a constant speed in a typical viscometer is a measurement of the instrument viscosity of a fluid (not the apparent viscosity). In the case of non-Newtonian fluids, measurement of apparent viscosity without knowledge of the shear rate is of limited value: the measurement cannot be compared to other measurements if the speed and geometry of the two instruments is not identical. An apparent viscosity that is reported without the shear rate or information about the instrument and settings (e.g. speed and spindle type for a rotational viscometer) is meaningless.

Multiple measurements of apparent viscosity at different, well-defined shear rates, can give useful information about the non-Newtonian behaviour of a fluid, and allow it to be modeled.

Power-law fluids

[edit]

In many non-Newtonian fluids, the shear stress due to viscosity, , can be modeled by

where

  • k is the consistency index
  • n is the flow behavior index
  • du/dy is the shear rate, with velocity u and position y

These fluids are called power-law fluids.

To ensure that has the same sign as du/dy, this is often written as

where the term

gives the apparent viscosity.[1]

See also

[edit]

References

[edit]
Revisions and contributorsEdit on WikipediaRead on Wikipedia

Apparent viscosity

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from Grokipedia
Apparent viscosity is a rheological property defined as the ratio of shear stress to shear rate for a fluid under specific flow conditions, serving as an effective measure of flow resistance in non-Newtonian fluids where true viscosity is not constant. Unlike Newtonian fluids, such as water or air, where viscosity remains independent of shear rate, apparent viscosity varies with the applied shear, reflecting the fluid's nonlinear response to deformation. This concept is mathematically expressed as μapp=τγ˙\mu_{app} = \frac{\tau}{\dot{\gamma}}, where τ\tau is the shear stress and γ˙\dot{\gamma} is the shear rate, allowing it to capture instantaneous flow behavior. In non-Newtonian fluids, apparent viscosity can decrease with increasing in shear-thinning (pseudoplastic) materials, such as paints, , or solutions, facilitating easier flow under stress like during application or circulation. Conversely, in shear-thickening () fluids, such as certain suspensions or cornstarch mixtures, it increases with , providing protective thickening under high impact. These behaviors are often modeled using the power-law equation τ=Kγ˙n\tau = K \dot{\gamma}^n, where KK is the consistency index and nn is the flow behavior index (n<1n < 1 for shear-thinning, n>1n > 1 for shear-thickening), enabling prediction of flow in engineering contexts. Apparent viscosity is crucial in fields like , , and , where it influences design of pipelines, systems, and product formulations by accounting for real-world flow variations rather than idealized constant . Measurement typically involves rheometers that apply controlled shear rates to plot curves, revealing the fluid's response across conditions. Understanding this property helps mitigate issues like pumping inefficiencies or inconsistent in industrial applications.

Fundamentals

Definition

Apparent viscosity, denoted as ηa\eta_a, is defined as the ratio of τ\tau to γ˙\dot{\gamma} at a specific flow condition. This measure treats the as if it were Newtonian for analytical purposes, even though the exhibits non-Newtonian . The basic equation for apparent viscosity is given by ηa=τγ˙,\eta_a = \frac{\tau}{\dot{\gamma}}, where it represents an instantaneous value that varies with the applied , providing a practical effective for complex fluids. This shear-rate-dependent quantity simplifies the analysis of non-Newtonian fluids, such as melts or suspensions, by allowing to approximate flow resistance under defined conditions without needing full rheological models. The term apparent viscosity emerged in early 20th-century studies, with significant developments by Eugene C. Bingham in the 1920s, who linked it to non-linear flow behaviors observed in yield stress materials like kaolin suspensions. In Newtonian fluids, apparent viscosity remains constant and equals the true , serving as a baseline for comparison.

Relation to and Rate

Shear stress, denoted as τ\tau, represents the tangential per unit area applied to a , driving its deformation and flow in a specific direction. This arises from interactions between layers sliding one another, such as in the transfer within a velocity gradient. Shear rate, symbolized as γ˙\dot{\gamma}, quantifies the rate of this deformation and is defined as the velocity gradient perpendicular to the flow direction, typically expressed in units of s⁻¹. It measures how rapidly adjacent layers move relative to each other, influencing the fluid's resistance to flow. In non-Newtonian fluids, the relationship between and deviates from the linear proportionality observed in Newtonian fluids, where stress is directly proportional to rate with a constant . Instead, this relationship is nonlinear, leading to variable flow resistance that depends on the imposed deformation. Apparent viscosity emerges as the ratio η=τ/γ˙\eta = \tau / \dot{\gamma}, providing an effective measure of at any given , though it is not constant across conditions. Flow curves, which plot against , illustrate these deviations vividly, often presented on a log-log scale to highlight the nonlinear behavior and power-law-like trends over wide ranges of deformation. On such log-log plots of τ\tau versus γ˙\dot{\gamma}, Newtonian fluids appear as straight lines with a of 1, whereas non-Newtonian fluids show curving or sloped lines indicating changing resistance. Apparent viscosity is determined as the secant from the origin to a specific point on the flow curve, i.e., the τ/γ˙\tau / \dot{\gamma}, quantifying the fluid's effective Newtonian-like response under those conditions. Pseudoplastic fluids, also known as shear-thinning materials, exhibit a decrease in apparent viscosity as increases, resulting in easier flow under higher deformation rates. Common examples include solutions and paints, where structural alignments or breakdowns reduce internal . In a log-log plot of apparent viscosity versus shear rate, this behavior manifests as a downward-sloping line, with viscosity dropping sharply at moderate to high γ˙\dot{\gamma} values before potentially plateauing. Conversely, dilatant fluids, or shear-thickening ones, display an increase in apparent viscosity with rising shear rate, as particle interactions or alignments stiffen the material. Such fluids, like certain suspensions of cornstarch in , show an upward-sloping line on the viscosity profile, where flow becomes more resistant under intense shearing. This concept of apparent viscosity serves as a foundational prerequisite for rheological modeling, as it captures the local, effective secant from the origin mimicking Newtonian on the nonlinear flow , enabling analysis of complex without assuming constancy.

Rheological Models

Power-Law Fluids

The power-law model, also known as the Ostwald-de Waele relationship, provides a foundational framework for describing the rheological of certain non-Newtonian fluids where the τ\tau relates nonlinearly to the γ˙\dot{\gamma}. In this model, the relationship is expressed as τ=Kγ˙n,\tau = K \dot{\gamma}^n, where KK is the consistency index (with units of Pa·sn^n) that characterizes the fluid's viscous properties, and nn is the dimensionless flow behavior index that determines the type of non-Newtonian response. For Newtonian fluids, n=1n = 1, reducing the model to τ=Kγ˙\tau = K \dot{\gamma} with constant viscosity. Values of n<1n < 1 indicate shear-thinning (pseudoplastic) behavior, where viscosity decreases with increasing shear rate, while n>1n > 1 denotes shear-thickening (dilatant) behavior, where viscosity increases. The apparent viscosity ηa\eta_a for power-law fluids is derived directly from the definition ηa=τ/γ˙\eta_a = \tau / \dot{\gamma}, yielding ηa=Kγ˙n−1.\eta_a = K \dot{\gamma}^{n-1}. This equation explicitly demonstrates the shear-rate dependence of , central to apparent viscosity in non-Newtonian contexts: for shear-thinning fluids (n<1n < 1), ηa\eta_a decreases as γ˙\dot{\gamma} increases (since n−1<0n-1 < 0), facilitating easier flow under stress; conversely, for shear-thickening fluids (n>1n > 1), ηa\eta_a rises with γ˙\dot{\gamma}, enhancing resistance. This dependence arises from the power-law assumption applied to the general shear stress-rate relation, making it a simple yet effective approximation for intermediate shear regimes. Representative examples illustrate the model's utility. Paints often exhibit shear-thinning behavior with n≈0.5n \approx 0.5, allowing high viscosity at low shear rates (e.g., γ˙=0.1\dot{\gamma} = 0.1 s−1^{-1}) for drip resistance, where ηa\eta_a might be around 32 Pa·s assuming K=10K = 10 Pa·sn^n, but dropping to 1 Pa·s at high shear (e.g., γ˙=100\dot{\gamma} = 100 s−1^{-1}) for smooth application. In contrast, cornstarch-water suspensions (typically 50-55 wt.% solids) display shear-thickening behavior, enabling phenomena like "walking on water" under impact. Despite its simplicity, the power-law model serves as an approximation with notable limitations, particularly at extreme shear rates. For shear-thinning fluids (n<1n < 1), it predicts infinite ηa\eta_a as γ˙→0\dot{\gamma} \to 0 and zero ηa\eta_a as γ˙→∞\dot{\gamma} \to \infty, which contradicts real fluids that approach finite Newtonian plateaus; thus, it is unreliable outside intermediate shear ranges where experimental data align with the power-law fit.

Cross and Carreau Models

The and Carreau models represent empirical rheological frameworks designed to describe the apparent viscosity of shear-thinning fluids that exhibit Newtonian plateaus at both low and high shear rates, extending beyond simpler unbounded models by incorporating asymptotic behaviors. These models are particularly valuable for complex fluids where transitions smoothly from a zero-shear value to an infinite-shear limit, enabling more accurate predictions across wide ranges encountered in practical flows. The Cross model, proposed by Malcolm M. Cross in , expresses the apparent viscosity ηa\eta_a as a function of γ˙\dot{\gamma} through the equation: ηa=η∞+η0−η∞1+([λ](/page/Lambda)γ˙)m\eta_a = \eta_\infty + \frac{\eta_0 - \eta_\infty}{1 + ([\lambda](/page/Lambda) \dot{\gamma})^m} Here, η0\eta_0 denotes the zero-shear , representing the Newtonian plateau at low s; η∞\eta_\infty is the infinite-shear , the lower at high shear; [λ](/page/Lambda)[\lambda](/page/Lambda) is a related to the onset of ; and mm (typically between 0 and 1) controls the sharpness of the transition. This four-parameter form allows fitting to experimental data via nonlinear least-squares optimization on logarithmic plots of versus , often yielding [λ](/page/Lambda)[\lambda](/page/Lambda) values on the order of 0.1–10 s for systems and mm around 0.5–0.8 to capture moderate transitions. The Carreau model, developed by Pierre J. Carreau in 1972, provides a similar but analytically smoother description, emphasizing molecular network theories for viscoelastic fluids: ηa=η∞+(η0−η∞)[1+(λγ˙)2](n−1)/2\eta_a = \eta_\infty + (\eta_0 - \eta_\infty) [1 + (\lambda \dot{\gamma})^2]^{(n-1)/2} In this equation, the parameters mirror those of the Cross model, with η0\eta_0 and η∞\eta_\infty as the viscosity limits, λ\lambda as the relaxation time, and nn (0 < n < 1) as the power-law exponent influencing the thinning slope in the intermediate regime. Parameter estimation follows a comparable nonlinear regression approach, frequently applied to capillary rheometer data, where nn values near 0.6–0.9 fit shear-thinning polymers, and λ\lambda scales with molecular weight. These models find application in modeling solutions, where the Cross equation effectively captures the shear-dependent of concentrated melts like , enabling predictions of flow in processes by fitting parameters to rotational measurements. In blood , the Carreau model simulates the non-Newtonian behavior of , accounting for aggregation at low shear (high η0\eta_0) and alignment at high shear (low η∞\eta_\infty), with typical showing η0≈0.056\eta_0 \approx 0.056 Pa·s, η∞≈0.0035\eta_\infty \approx 0.0035 Pa·s, λ≈3.313\lambda \approx 3.313 s, and n≈0.3568n \approx 0.3568 for physiological conditions. Such outperform unbounded alternatives in extremes, as power-law approximations hold only in intermediate shear regimes without capturing the plateaus. A key advantage of the Cross and Carreau models over the power-law is their incorporation of bounded Newtonian limits, preventing unphysical divergences at low shear (where power-law predicts infinite viscosity) and ensuring finite high-shear values, thus improving accuracy for broad-range simulations in processing and hemodynamic flows. This asymptotic fidelity enhances predictive reliability when extrapolating beyond measured data, as validated in fits to diverse experimental datasets.

Measurement Techniques

Viscometry Methods

Viscometry methods provide essential laboratory techniques for quantifying apparent (η_a) in non-Newtonian fluids by imposing controlled shear flows and measuring the ratio of (τ) to (γ̇), where η_a represents an effective at specific conditions. These approaches allow construction of flow curves—plots of τ versus γ̇ or η_a versus γ̇—to characterize shear-dependent behavior across a range of rates. Capillary viscometry adapts Poiseuille's law for non-Newtonian flows by forcing the fluid through a cylindrical tube of radius R and length L, using the ΔP and Q to compute wall and apparent . The wall is given by τ_w = (ΔP R) / (2 L), independent of fluid , while the apparent at the wall is γ̇_a = 4 Q / (π R^3); thus, η_a = τ_w / γ̇_a yields the apparent viscosity at this nominal rate. For non-Newtonian fluids, the velocity profile deviates from parabolic, requiring the Rabinowitsch correction to obtain the true wall : γ˙w=γ˙a(34+14dln⁡γ˙adln⁡τw)\dot{\gamma}_w = \dot{\gamma}_a \left( \frac{3}{4} + \frac{1}{4} \frac{d \ln \dot{\gamma}_a}{d \ln \tau_w} \right) This correction, derived from integrating the momentum balance, accounts for the non-uniform shear across the radius and enhances accuracy for pseudoplastic or dilatant behaviors. Rotational viscometers employ geometries like Couette (concentric cylinders) or cone-plate to generate simple shear, measuring torque as a function of angular velocity to derive η_a. In a narrow-gap Couette setup, the inner cylinder rotates at angular velocity Ω while the outer remains stationary; the nominal shear rate is γ̇ ≈ (R_i Ω) / (R_o - R_i), where R_i and R_o are inner and outer radii, and shear stress τ = M / (2 π R_i^2 h) with torque M and gap height h, allowing η_a = τ / γ̇. Cone-plate geometry maintains constant γ̇ = Ω / α throughout the small cone angle α, minimizing edge effects and providing uniform stress distribution, which is particularly suitable for low-viscosity or shear-thinning non-Newtonian fluids. Standard procedures involve steady-state measurements, where the system equilibrates at constant applied stress or rate until torque or pressure stabilizes, typically over several minutes per point, across a decade or more of γ̇ values to generate comprehensive flow curves. Common error sources include wall slip, where the fluid detaches from the surface due to weak adhesion in suspensions or polymers, artificially lowering measured τ and η_a; this is mitigated by using roughened walls or multiple capillary diameters to extrapolate true values. The evolution of these methods traces to Eugene C. Bingham's 1916 capillary experiments on yield-stress materials like paints, adapting Poiseuille's framework to non-Newtonian "plastic" flow despite initial assumptions of Newtonian-like profiles. Refinements, such as the Rabinowitsch correction, addressed profile distortions, paving the way for modern automated capillary rheometers that integrate precise drives, transducers, and software for real-time corrections and .

Rheometer Applications

Rheometers enable precise measurement of apparent viscosity (η_a) in settings by operating in two primary modes: controlled-stress and controlled-rate. In controlled-stress mode, a constant or varying stress is applied to the sample, allowing the instrument to measure the resulting strain or , which is particularly useful for probing low-stress behaviors and yield stresses in complex fluids where η_a may vary nonlinearly with deformation. Conversely, controlled-rate mode imposes a specified or strain, measuring the corresponding stress response, which facilitates direct calculation of η_a = τ / γ̇ for steady shear flows and is ideal for high-shear regimes encountered in melts or suspensions. These modes can be applied under both steady shear and oscillatory conditions, with oscillatory tests providing dynamic moduli (G' and G'') from which the complex |η*| is derived, offering insights into viscoelastic contributions to apparent viscosity without inducing structural breakdown. Advanced protocols such as creep recovery and stress relaxation further refine the profiling of time-dependent apparent viscosity in non-Newtonian materials. Creep recovery involves applying a constant stress to induce deformation (creep phase), followed by stress removal to observe (recovery phase), allowing researchers to quantify recoverable strain and viscous dissipation, which inform the time-dependent evolution of η_a in thixotropic or viscoelastic fluids. , by contrast, applies a fixed strain and monitors the decay in stress over time, revealing relaxation times that characterize how η_a approaches zero-shear limits in entangled systems like solutions. These techniques are essential for inferring η_a in scenarios where steady-state assumptions fail, such as in yield-stress fluids, by separating elastic and viscous components through compliance functions J(t). Data processing in rheometry often employs master curves and the Cox-Merz rule to correlate steady and dynamic measurements, enhancing the predictive power for apparent across wide ranges. Master curves are constructed via time-temperature superposition, shifting isothermal data to a reference to generate a broad-spectrum profile, which captures η_a over inaccessible experimental timescales in materials like amorphous . The Cox-Merz rule empirically links the steady-shear apparent η(γ̇) to the magnitude of the complex |η*(ω)| by equating them when ω replaces γ̇, enabling estimation of nonlinear steady-shear data from linear oscillatory tests—a validation observed in numerous monodisperse systems. This superposition facilitates model fitting for rheological constitutions without exhaustive experimentation. In the 2020s, microfluidic rheometers have advanced apparent viscosity measurements for minuscule samples, particularly in fluids like nanofluids and suspensions, requiring volumes as low as microliters. These devices integrate microchannels with pressure-driven flows to achieve high shear rates (up to 10^6 s^-1) while minimizing sample use, ideal for scarce where traditional rheometers demand milliliters. For instance, in dispersions, microfluidic setups reveal shear-thinning η_a profiles influenced by particle alignment, aiding optimization of conductivity enhancements in nanofluids. Such innovations, often combining optical or electrical detection, extend rheometric precision to emerging fields like nano-enhanced lubricants, where apparent viscosity dictates flow stability at microscales.

Practical Applications

Industrial Processes

In industrial pumping and piping systems, apparent viscosity plays a critical role in handling shear-thinning non-Newtonian fluids, such as melts during processes. Shear-thinning behavior, where apparent viscosity decreases with increasing , allows for reduced pressure drops and lower in pumping operations by facilitating easier flow at higher velocities typical of industrial pipelines. For instance, in , this property minimizes power requirements, as higher screw speeds induce greater s that lower the effective viscosity, thereby enhancing throughput while reducing operational costs. To predict flow regimes in such systems, engineers employ a generalized adapted for non-Newtonian fluids, which incorporates apparent viscosity derived from models like the Herschel-Bulkley extended form to account for yield stress and shear-dependent effects, enabling accurate design of laminar-to-turbulent transitions in networks. In , apparent viscosity governs the efficiency of mixing and for complex fluids like sauces and , which often exhibit shear-thinning characteristics. For sauces, such as tomato-based formulations, higher apparent viscosity at low shear rates ensures stability during storage and prevents , while shear-thinning during mixing reduces energy input and improves homogeneity by allowing easier incorporation of ingredients under agitation. In dough , ingredients like or oils influence apparent viscosity, directly impacting extrusion rates; for example, stable viscosity profiles under high-shear conditions in twin-screw extruders promote uniform product expansion and consistent output, optimizing production lines for baked goods or . These properties are often approximated using the power-law model for rapid process adjustments. In the oil and gas sector, specialized shear-thickening additives, such as deformable particles or certain polymers, are incorporated into otherwise shear-thinning drilling fluids to exhibit dilatant behavior under high shear, increasing viscosity to form a robust seal and prevent lost circulation into fractured formations. These additives trigger rapid viscosity buildup at the bit or loss zones, bridging fractures and minimizing fluid invasion while maintaining pumpability at lower shears during circulation. This approach enhances drilling safety and efficiency without compromising overall fluid rheology. Optimization strategies in leverage tailored apparent viscosity profiles to boost throughput and product quality, as seen in formulation case studies. By adjusting rheology modifiers to achieve desired shear-thinning or yield stress characteristics, formulators ensure paints flow easily during high-shear application (e.g., spraying) while resisting sagging at low shear, thereby increasing application and reducing waste. Such targeted apparent viscosity engineering, often informed by , minimizes energy use in mixing and while maximizing output in coatings .

Biomedical Uses

In biomedical contexts, apparent viscosity plays a crucial role in the of , a whose apparent viscosity decreases with increasing due to the deformation and alignment of red blood cells (RBCs), which reduces internal friction and enhances flow efficiency. This shear-thinning behavior is particularly evident in the , where the Fåhræus-Lindqvist effect further lowers apparent viscosity in small vessels (diameters below 300 μm) as RBCs migrate axially, forming a cell-free marginal layer that minimizes wall interactions and apparent resistance to flow. The Cross model effectively captures this transition, describing blood's apparent viscosity as approaching a Newtonian limit at high shear rates above approximately 100 s⁻¹, where RBC alignment dominates over aggregation. Apparent viscosity is leveraged in drug delivery systems through shear-thinning hydrogels, which exhibit high viscosity at rest to form stable depots in tissues but reduce apparent viscosity dramatically under the high shear of injection needles, enabling minimally invasive administration. For instance, hyaluronic acid-based gels demonstrate this property, with apparent viscosity dropping by orders of magnitude at shear rates exceeding 100 s⁻¹ during extrusion, allowing easy flow through 25-gauge needles while rapidly recovering post-injection to encapsulate therapeutics like chemotherapeutics or biologics over weeks. This design improves patient compliance and targeted release, as seen in formulations for ocular or subcutaneous delivery where sustained viscosity post-injection prevents premature diffusion. In , apparent viscosity of is modeled to develop biomimetic lubricants that replicate its shear-thinning characteristics, ensuring low during motion while providing load-bearing support at rest. 's apparent viscosity, primarily from high-molecular-weight hyaluronan and lubricin, decreases under shear rates typical of walking (10-100 s⁻¹), facilitating boundary of surfaces and reducing in engineered constructs. Researchers engineer scaffolds with tunable apparent viscosity, such as hyaluronan composites, to mimic this for treatments, where viscosupplementation restores and promotes tissue regeneration without inflammation. Recent 2020s research highlights how alters respiratory apparent viscosity, increasing it through hypersecretion and , which impairs ciliary clearance and airflow in airways. Studies from 2021-2024 show that infected patients' exhibits elevated apparent viscosity (up to 10-100 times normal at low shear rates below 1 s⁻¹), forming plugs that elevate and reduce expiratory flow rates by 50% or more, contributing to ventilation-perfusion mismatches and severe . This viscoelastic stiffening, driven by MUC5AC overproduction, links directly to prolonged needs, prompting therapies like mucolytics to restore shear-dependent flow.

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