Local flow topology of a polymer-laden turbulent boundary layer

Abstract Fine-scale flow motions are measured in a Newtonian and polymer drag-reduced turbulent boundary layer (TBL) at a common momentum thickness Reynolds number $Re_{\theta }$ of 2300. Relative to the Newtonian TBL, the polymer-laden flow has a 33 % lower skin-friction coefficient. Three-dimensional (3-D) particle tracking velocimetry is used to measure the components of the velocity gradient tensor (VGT), rate of deformation tensor (RDT) and rate of rotation tensor (RRT). The invariants in these tensors are then used to distinguish the different types of fine-scale flow motions – a method called the $\varDelta$-criterion. Joint probability density functions (j.p.d.f.s) of the VGT invariants, $Q$ and $R$, for the Newtonian TBL produce the familiar tear-drop pattern, commonly seen in direct numerical simulations of Newtonian turbulence. Relative to the Newtonian TBL, the polymer-laden flow has significantly attenuated values of $R$, implying an overall reduction in fluid stretching. The invariants in the RDT, $Q_D$ and $R_D$, imply that straining motions of the polymeric flow are more two dimensional compared with the Newtonian flow. Moreover, j.p.d.f.s of $Q_D$ and the invariant in the RRT $Q_W$, suggest that the flow consists of fewer biaxial extensional events and more shear-dominated flow. Few, if any, experimental investigations have measured the 3-D structure of fine-scale motions in a Newtonian and polymer drag-reduced TBL using the $\varDelta$-criterion. We provide the first experimental evidence that supports the notion that an attenuation of fluid stretching, particularly biaxial straining motions, is central to the mechanism of polymer drag reduction.


Introduction
It is well known that turbulent wall-bounded flows of high molecular weight polymer solutions can have significantly less skin-friction drag than Newtonian fluids at a similar Reynolds number.Since its discovery by Toms (1948), the phenomenon of polymer drag reduction (DR) has garnered considerable attention (Lumley 1969;Procaccia, L'vov & Benzi 2008;White & Mungal 2008;Graham 2014;Xi 2019); yet, the fundamental question of how polymers reduce drag remains elusive.An incomplete understanding of the mechanism of DR can be attributed to the complexity of the turbulent flow, coupled with the complexity of the polymer solution and its non-Newtonian constitutive equation (White & Mungal 2008).Revealing the mechanics of polymer DR requires comparisons between experiments that accurately measure the fluctuating velocity field of polymer drag-reduced wall flows, and numerical simulations that utilize non-Newtonian constitutive models.Antiquated works generally involved interpretations of various ensemble statistics, such as mean velocity and Reynolds stresses.While the focus of more recent investigations has shifted towards understanding the distribution and evolution of coherent flow structures -an analysis propelled almost entirely by works using numerical simulations (Xi 2019).Experiments have trailed in this regard, most likely due to the tremendous difficulties involved with measuring coherent structures.Therefore, the broad goal of the present investigation is to determine the three-dimensional (3-D) topology of the turbulent motions within a polymer-laden boundary layer using modern flow measurements.
There are several methods for identifying the topology of the turbulent motions.The present work utilizes that of Chong, Perry & Cantwell (1990), herein referred to as the Δ-criterion, where Δ is defined as the discriminant of the characteristic equation for the velocity gradient tensor (VGT).The Δ-criterion utilizes the eigenvalues and invariants of the VGT to identify the local topology and streamline patterns about critical points within the flow.Examples of flow topologies include those that are focal (vortical) and dissipative (saddle points), depending on the sign of the invariants and the real/complex nature of the eigenvalues.Using the Δ-criterion, various works have demonstrated that quasi-streamwise and hairpin vortices can be visualized in numerical simulations and flow measurements of Newtonian wall-bounded turbulence (Blackburn, Mansour & Cantwell 1996).Furthermore, the joint probability density function (j.p.d.f.) of the invariants in the VGT takes on a tear-drop or pear-shaped distribution.This tear-drop pattern in the j.p.d.f. of the VGT invariants is not only found in wall-bounded turbulence (Blackburn et al. 1996;Chacín, Cantwell & Kline 1996;Chong et al. 1998;Chacín & Cantwell 2000;Elsinga & Marusic 2010), but also turbulent mixing layers (Soria et al. 1994;Buxton, Laizet & Ganapathisubramani 2011), jets (da Silva & Pereira 2008;Buxton & Ganapathisubramani 2010) and isotropic turbulence (Martın et al. 1998;Ooi et al. 1999;Danish & Meneveau 2018), implying a universal distribution of topologies exists among different types of Newtonian turbulence.
Few investigations have used the Δ-criterion to explore the distribution of flow topologies in wall-bounded turbulence with non-Newtonian rheology (Mortimer & Fairweather 2022).The work by Mortimer & Fairweather (2022) observed an unambiguous change in the topology of a viscoelastic channel flow at a friction Reynolds number Re τ of 180, and derived from direct numerical simulation (DNS) utilizing the FENE-P constitutive model.Here, FENE-P stands for finitely extensible nonlinear elastic dumbbells with the Peterlin approximation.Mortimer & Fairweather (2022) demonstrated that drag-reduced channel flows have a narrower range in the third invariant of the VGT and flow structures were more two dimensional, relative to Newtonian channel flows at a similar Re τ .Despite these observations, the flows investigated by Mortimer & Fairweather (2022) had very low DR percentages (less than 5 %) and modest non-Newtonian rheology, with negligible shear thinning and relatively low amounts of elasticity compared with other numerical investigations of drag-reduced flows (Xi 2019).Therefore, it is unclear what the topology based on the Δ-criterion would look like for flows with larger amounts of DR, let alone a flow that utilizes a realistic polymer solution that is shear thinning and viscoelastic.
While the Δ-criterion has not been employed to investigate the topology of polymer drag-reduced flows with large amounts of DR, it has been used to assess the topology of low-Reynolds-number transitional channel flows exhibiting elasto-inertial turbulence (EIT).Samanta et al. (2013) observed that below the critical Reynolds number for laminar-turbulent transition, polymer-laden pipe and channel flows exhibit an early transition to a different type of disordered motion referred to as EIT.Numerical simulations of channel flows utilizing the FENE-P constitutive model have demonstrated that EIT is inherently two dimensional and consists of alternating regions of vortical and dissipative flow (i.e.positive and negative Δ) along the streamwise direction (Samanta et al. 2013).In the j.p.d.f. of the VGT invariants, EIT reflects a symmetric ovular pattern that is significantly different than the tear-drop pattern observed in Newtonian turbulence (Dubief, Terrapon & Soria 2013).The connection between EIT and DR, and whether it persists at much larger Reynolds numbers, is still unknown (Xi 2019).Therefore, comparing the measured topology of a polymer drag-reduced flow with the known topology of EIT derived from viscoelastic simulations could provide evidence that EIT contributes to the dynamics at larger Reynolds numbers.
Although few works have used the Δ-criterion to characterize the topology of polymer drag-reduced flows, observations of coherent structures have been performed using other techniques.For example, Pereira et al. (2017) utilized a modified Q-criterion, or the second invariant in the VGT (Hunt, Wray & Moin 1988;Martins et al. 2016), to discern vortical and extensional structures in channel flow DNS with the FENE-P constitutive model, an Re τ between 180 and 1000, and DR as large as 62 %.Pereira et al. (2017) noted that both extensional and vortical flow motions in the drag-reduced channel flow were weaker relative to Newtonian DNS, and the flow tended towards a more parabolic (shear-dominant) state -a trend Pereira et al. (2017) referred to as 'flow parabolization'.An earlier investigation by Roy et al. (2006) similarly implied flow parabolization based on channel flow simulation that utilized a simplified constitutive model of polymer stresses (the retarded-motion expansion).Roy et al. (2006) more specifically asserted that the non-Newtonian extensional viscosity opposed flow in both uniaxial and biaxial flow regions, thus mitigating the strength and formation of quasi-streamwise vortices and reducing drag.Many of the previously listed numerical investigations (Roy et al. 2006;Pereira et al. 2017;Mortimer & Fairweather 2022) provide meaningful assertions about the influence of polymer rheology on flow topology; however, all of these works utilize constitutive models, such as FENE-P, that only approximate polymer-driven stresses (Xi 2019) and few experiments have measured the topology of a polymer drag-reduced flow to corroborate these observations.
Early experimental investigations made inferences about the size of large-scale motions in polymer drag-reduced flows based on measurements using two-dimensional (2-D) particle image velocimetry (PIV) and two-point velocity statistics.One such notable experimental work was that of White, Somandepalli & Mungal (2004), which investigated a drag-reduced boundary layer with near-wall injection of a concentrated polymer solution, a momentum thickness-based Reynolds number Re θ of 1300 to 1400 and DR between 33 % and 67 %.Within the buffer layer of the flow, White et al. (2004) observed visibly wider and longer high-and low-speed velocity streaks for a flow with DR of 50 % relative to water at a similar Re θ .Two-point spatial correlations of the streamwise velocity fluctuations along the spanwise direction confirmed that the large-scale motions became increasingly wider as DR grew from 33 % to 67 %.A similar widening and elongation of the large-scale motions was observed for drag-reduced boundary layers of homogeneous polymer solutions (often referred to as a polymer ocean) by Farsiani et al. (2020), and also homogeneous polymer drag-reduced channel flows by Warholic et al. (2001) and Warwaruk & Ghaemi (2021).In addition to velocity correlations, White et al. (2004) also observed a reduction in the strength and number of near-wall vortices, albeit inferred from visualization of an instantaneous snapshot of the wall-normal vorticity.From an experimental perspective, the natural progression to the work of White et al. (2004) is to better quantify the near-wall vortical structures of a polymer drag-reduced flow using 3-D flow measurements and a suitable method for detecting such structures.
A limited number of experimental investigations have used 3-D flow measurements to measure the velocity in polymer drag-reduced flows, let alone one that quantifies the topology of fine-scale motions within the flow.Shah, Ghaemi & Yarusevych (2021) performed 3-D tomographic PIV on a polymer drag-reduced boundary layer with heterogeneous wall injection, an Re θ of 520 and DR of 20 %-30 %.Using a modified Q-criterion (Hunt et al. 1988;Martins et al. 2016), Shah et al. (2021) demonstrated that extensional and vortical flow regions weaken as drag was reduced, similar to the findings of the numerical investigation by Pereira et al. (2017).Rather than Q-criterion, the current work expands on the experimental findings of Shah et al. (2021) by utilizing the Δ-criterion to obtain distributions, mainly j.p.d.f.s, of the different types of topologies within a Newtonian and polymer-laden turbulent boundary later (TBL).Compared with the Q-criterion, use of the Δ-criterion, as well as other deformation tensor invariants, facilitates a more complete depiction of the topology of fine-scale motions within the turbulent drag-reduced flow.Unlike the use of just Q, considering the other tensor invariants and Δ can help distinguish structures that are in uniaxial or biaxial extension, as well as focal or dissipative; some of which are significant to the mechanism for polymer DR.
In the present investigation, the VGT of a polymer drag-reduced boundary layer will be measured using state-of-the-art 3-D particle tracking velocimetry (3-D-PTV), from which the local flow topology will be analysed using the Δ-criterion.Evidence is provided to test a hypothesis regarding the mechanism of polymer DR.This hypothesis is inspired by the works of Roy et al. (2006) and Lumley (1973) -that being, the large extensional viscosity of polymer solutions strongly inhibits uniaxial and biaxial flow regions, thus mitigating the strength and formation of quasi-streamwise vortices and reducing drag.It is clear that even small amounts of DR will produce an unambiguous change in the topology of a TBL (Pereira et al. 2017;Mortimer & Fairweather 2022); however, based on the findings of Roy et al. (2006), it is expected that changes in the topology will predominately occur in regions of strong uniaxial/biaxial extension.Uniaxial/biaxial flow regions are dissipative with Δ < 0, and are strongly concentrated around the 'tails' in the j.p.d.f. of the VGT invariants.They can also be identified from the invariants in the rate of deformation tensor (RDT) or the symmetric component of the VGT, which will be elaborated upon more in § 2 to follow.

Theoretical background
The following section will serve to summarize the Δ-criterion of Chong et al. (1990).This method utilizes the eigenvalues and invariants of the VGT to identify the local topology and streamline patterns of the flow.The VGT is L = ∇U and U is the velocity vector.The

Unstable focus compressing
Unstable nodesaddle-saddle Stable nodesaddle-saddle Local topologies for different R and Q in an incompressible flow with P = 0 (Chong et al. 1990).
characteristic equation for the tensor L is where P, Q and R are the invariants of L. The eigenvalues are the roots to (2.1), and are defined as Λ 1 , Λ 2 and Λ 3 in descending order of magnitude.Although the Δ-criterion can be applied to both compressible and incompressible fluid flows, the present work focuses only on those that are incompressible, thus narrowing down the number of flow classifications.In an incompressible flow, the first invariant P = −tr(L) is equal to zero, while Q and R are the only non-zero invariants of L and can be expressed as Here, tr(. . . ) represents the trace operator on a square matrix and det(. . . ) the determinant.
The nature of the eigenvalues of L are dictated by the sign convention of the discriminant Δ of (2.1), where Δ > 0 produces one real and two complex eigenvalues, and Δ ≤ 0 produces three real eigenvalues.Figure 1 describes the different possible local flow topologies that depend on the sign convention of Δ and R (Chong et al. 1990).The lines corresponding to Δ = 0, and shown in figure 1, are referred to as the Vieillefosse tail's.Here, (Δ = 0, R < 0) is the left-Vieillefosse tail and (Δ = 0, R > 0) is the right-Vieillefosse tail.Flow conditions above the Vieillefosse tail's with Δ > 0, consist of motions that are focal and primarily vortical.Regions of the flow with Δ ≤ 0 take on a node-saddle-saddle streamline pattern.Flow topology is also divided about the R = 0 axis, where flows with R < 0 are stable (stretching) and R > 0 are unstable (compressing).The j.p.d.f.s of Q and R in various Newtonian turbulent flows take on a tear-drop pattern (Soria et al. 1994;Blackburn et al.  (Blackburn et al. 1996).
1996; Chong et al. 1998;Ooi et al. 1999;da Silva & Pereira 2008).The point or tip of the tear-drop falls on the right-Vieillefosse tail (Δ = 0, R > 0), while the bulb of the tear drop is situated in the quadrant of stable focus stretching (Δ > 0, R < 0).The VGT indicated as L can be separated into a symmetric and antisymmetric component, where L = D + W .Here the symmetric RDT is D = (∇U + ∇U † )/2, the antisymmetric rate of rotation tensor (RRT) is W = (∇U − ∇U † )/2, and the dagger symbol † represents the matrix transpose.Similar to L, the tensors D and W have their own characteristic equation.For the tensor D, the characteristic equation is (2.4) where P D = −tr(D) = 0 for an incompressible flow, and the non-zero invariants are defined according to The roots of (2.4) are the eigenvalues of D and are defined as Γ 1 , Γ 2 and Γ 3 in descending order of magnitude.Similar to (2.3) for L, the discriminant of (2.4) for D is Because D is a real and symmetric tensor, its eigenvalues will always be real and Δ D ≤ 0. A plot of Q D , R D space is shown in figure 2, where black solid lines represent curves with the same ratio of principal strain rates or eigenvalue of D, defined as Γ 1 : Γ 2 : Γ 3 (Blackburn et al. 1996).The ratio of principal strains are also used to distinguish possible rheometric flows, e.g.uniaxial extension, biaxial extension, planar extension and shear.A review of these basic rheometric flows is not presented, however deriving their respective Q W ∝ enstrophy density (2.7) For any antisymmetric tensor, the determinant is equal to zero; therefore, the third invariant of W , defined as R W , will always be zero.Also note that the second invariant of L can be equally represented as Values of Q D are always negative, while values of Q W are always positive.The invariants, Q D and Q W , are also proportional with energy dissipation ε = 2ν tr(D 2 ) = −4νQ D and enstrophy density φ = −2 tr(W 2 ) = 4Q W , where ν is the kinematic viscosity.Therefore, the ratio between Q W and Q D can indicate whether the flow is more dominated by dissipation or enstrophy.Truesdell (1954) established a kinematical vorticity number which defines the local strength of rotation relative to stretching (Ooi et al. 1999).The change in K is shown schematically in figure 3 for different Q D and Q W , similar to the diagram provided in Soria et al. (1994).Regions of the flow with small Q W and K ≈ 0 are more irrotational and dominated by dissipative motions, while flow regions with negligible Q D and large values of K that approach ∞ experience solid body rotation.
Regions with both large enstrophy density and dissipation fall on the line with K = 1, where Q W = −Q D .From simulations of an incompressible mixing layer, Soria et al. (1994) described how flow motions with K = 1 consist of vortex sheets and shear layers.
Comparing the invariants Q W and Q D is also commonly used to distinguish rheometric flows.Astarita (1979) derived a criteria that was adapted from the work of Astarita (1967), for distinguishing steady shear, extension and solid body rotation in non-Newtonian flows and served functionally the same as the kinematical vorticity number K. Flow regions that are extension dominant (K = 0), shear dominant (K = 1) or in rigid body rotation (K = ∞) are annotated on the schematic of Q D , Q W space shown in figure 3. Dimensionless indicators similar to K are generally referred to as a 'flow type' and can be commonly found in a variety of works involving non-Newtonian flows (Haward, McKinley & Shen 2016;Haward, Toda-Peters & Shen 2018;Ekanem et al. 2020;Walkama, Waisbord & Guasto 2020;Kumar, Guasto & Ardekani 2022).

Experimental methodology
The invariants in the VGT of a Newtonian and polymer-laden TBL were computed using velocity vectors measured from 3-D-PTV based on the shake-the-box (STB) algorithm developed by Schanz, Gesemann & Schröder (2016).Newtonian and polymer-laden flows were compared at a similar friction Reynolds number Re τ and momentum thickness Reynolds number Re θ .A detailed description of the flow facility, polymer solution, measurement apparatus and flow computations are provided in the following sections.
3.1.Flow facility Newtonian and polymer-laden TBLs were formed along the floor of a closed-loop water flume at the University of Alberta's Laboratory of Turbulent Flows (Abu Rowin, Hou & Ghaemi 2018;Elyasi & Ghaemi 2019).The flume consists of a 5 m long channel that bridges two cubic reservoirs.The channel was 0.68 m in width W. The free surface was situated at a height H that was 0.2 m above the bottom floor of the channel.The total volume of liquid within the flume was 3500 l.The walls of the channel consist of 12.7 mm thick glass panels.Two centrifugal pumps (Deming 4011 4S, Crane Pumps and Systems) in a parallel configuration were used to circulate the fluid within the flume.Variable frequency drive's enabled control of the rotational speed of each pump.In all experiments both pumps were operated at the same rotational speed.Measurements of the TBL of water were collected for pump speeds between 450 and 600 rpm, which corresponds to free-stream velocities U ∞ of 0.186 and 0.247 m s −1 .These values of U ∞ produce Newtonian flows with similar Re τ and Re θ as the polymer-laden flow, respectively.A series of mesh screens within the upstream reservoir of the water flume ensured that the turbulence intensity of the free stream was less than 2 %.Such a turbulence intensity was previously shown to not have a substantial influence on the inner-normalized mean velocity and Reynolds stress profiles near the wall, and is assumed to not have significant impact on the present results (Hancock & Bradshaw 1983, 1989).Fluid temperature was monitored using a K-type thermocouple and a data logger (HH506, Omega Engineering).Throughout all experiments, involving both water and the polymer-laden flows, the temperature was 19.9 • C ± 0.3 • C.

Polymer solution preparation and characterization
The flexible polymer polyacrylamide (PAM) (6030S, SNF Floerger) with a molecular weight of 30-35 MDa, was chosen for the polymer-laden boundary layer experiments.A 3500 l homogeneous PAM solution with a concentration c of 140 ppm was utilized.To prepare the polymer solution, a 1140 l concentrated master solution (c = 430 ppm) was first mixed and then diluted to achieve the desired 140 ppm concentration within the flume.The master solution was mixed in two 570 l cylindrical vessels.Solid polymer powder was weighed using a scale with a 0.1 g resolution, and gently added to each container (245 g to each vessel) along with tap water.A stand mixer equipped with a 150 mm diameter impeller and set to a rotational speed of 50 rpm was used to mix the master solution in each vessel for 2 h.The master solution was then slowly added to 2360 l of tap water that was contained within the flume.An air operated diaphragm pump was used to gently transfer the master solution from the mixing containers to the flume at a flow rate of 1 l s −1 .Upon adding the master solution to the flume, the 3500 l solution was then circulated for 30 min, where the rotational speed of the centrifugal pumps was set to a low speed of 300 rpm.The 140 ppm solution was then left to rest for 12 h.The resulting fluid was visibly transparent and had no heterogeneous clumps of polymers.
Flow measurements were performed immediately after the PAM solution was left to rest for 12 h.The rotational speed of the pumps were set to 1000 rpm, which produced a U ∞ of 0.432 m s −1 .To avoid degradation of the PAM solution, the pumps were turned off intermittently between instances of image acquisition for 3-D-PTV.For a single set of flow measurements, the pumps were turned on for 2 min.After which, the pumps were turned off for approximately 10 min to allow time for the 3-D-PTV images to be transferred from the on-board memory of the high-speed cameras to computer storage.Eight sets of images were collected for 3-D-PTV, therefore, this procedure of turning the pumps on for 2 min and off for 10 min was repeated eight times.Fluid samples were collected for rheology measurements immediately after each instance of image acquisition (eight fluid samples in total).Rheology measurements were necessary for characterizing the material properties of the fluid (i.e.shear viscosity and extensional relaxation time) and were also useful for diagnosing the effects of degradation.
The shear and extensional rheology of water and the 140 ppm PAM solution is provided in Appendix A. Torsional rheometry was used to measure the viscosity η as a function of shear rate γ for water and the eight samples of the PAM solution.Water exhibited a viscosity that was independent of γ and equal to 0.98 cP.On the other hand, the PAM solution was shear thinning, where measurements of η decreased with increasing γ .The shear-thinning trend was described by a Carreau model (Carreau 1972) with a zero-shear-rate viscosity η 0 of 3.4 cP, an infinite-shear-rate viscosity η ∞ of 1.0 cP, a consistency K of 0.29 s and a flow index m of 0.76.The total relative uncertainty in the measurements of η attributed to both systematic errors from the torsional rheometer and a repeatability error from polymer degradation was 5.3 % and considered minimal.The extensional rheology of water and PAM was evaluated using a bespoke apparatus that measured the diameter of a droplet expelled from a blunt-end nozzle using a high-speed camera and back light illumination (Deblais et al. 2020;Rajesh, Thiévenaz & Sauret 2022).Water exhibited a rapid decay in its droplet diameter representative of inertiocapillary dominated thinning.The droplet of the PAM solution had a much longer lifetime due to elastic forces.Based on the trend in the diameter of the thinning droplet, it was assessed that the PAM solution had an elastic relaxation time t e of 9.90 ms.

Flow measurements
Two types of flow measurements were used to characterize the Newtonian and non-Newtonian TBLs.The first was 3-D-PTV based on the STB algorithm (Schanz et al. 2016), which was used primarily to obtain the VGT.The second consisted of a two-camera planar PIV set-up, that was used to obtain bulk properties of the flow, including U ∞ , the momentum thickness θ and the boundary layer thickness δ.These measurements were done simultaneously, as described in the following sections.

Three-dimensional PTV
To obtain 3-D measurements of the velocity vector U within the Newtonian and non-Newtonian TBLs, 3-D-PTV using the STB algorithm was used (Schanz et al. 2016).The 3-D-PTV measurements produce Lagrangian trajectories of tracer particles that travel through the measurement domain.The STB algorithm can detect and track a larger number of tracer particles by utilizing temporal information over several successive images as opposed to standard double-frame 3-D-PTV algorithms (Wieneke 2012;Schanz et al. 2016).The velocities of the Lagrangian trajectories are then projected onto an Eulerian grid at each instance of time t.This effectively produces 3-D time-resolved measurements of U.
An isometric view that illustrates the 3-D-PTV measurement apparatus, with reference to a section of the water channel, is shown in figure 4(a).The 3-D-PTV measurement apparatus consisted of four high-speed cameras (Phantom v611, Vision Research Inc.), each of which is labelled from 1 to 4 in figure 4. A high-repetition Nd:YLF laser (DM20-527, Photonics Industries), with a wavelength of 532 nm and a maximum pulse energy of 20 mJ pulse −1 , was used to illuminate the volume of interest (VOI).A zoomed-in depiction of the VOI is shown in figure 4(b) with reference to the Cartesian coordinate system, where x, y and z are the streamwise, wall-normal and spanwise directions, respectively.The centre of the laser volume was positioned such that the VOI was at the channel mid-span (W/2) along z and 4.5 m downstream of the inlet to the water channel along x.The cropped laser volume was 3.5 mm thick along z and approximately 15 mm in width along x, and had a rather uniform intensity profile along those respective directions.
Each of the four high-speed cameras had a complementary metal oxide semiconductor sensor, that was cropped to be 1280 × 304 pixels in size, where each pixel was 20 × 20 µm 2 large and had a 12 bit digital resolution.The four cameras were arranged in a half-cross-like configuration, as depicted in figure 4(a).All cameras were placed in a portrait orientation such that the 1280 pixel dimension of each sensor was parallel to the y direction.The viewing angles of each camera with respect to the VOI are shown in figure 4(c,d).Water-filled prisms helped mitigate image distortion caused by light refraction for cameras 1, 3 and 4, which had large viewing angles with respect to the glass wall.Sigma lenses with a focal length f of 105 mm and 2× teleconverters (Teleplus pro300, Kenko) were used to achieve a magnification of approximately 0.72 for all four of the cameras.All cameras had a lens aperture of f /16, with an approximated depth of focus of 7 mm.Schiempflug adapters were also used for cameras 1, 3 and 4 to ensure images of the VOI were in focus.The cameras and laser were synchronized using a programmable timing unit (PTU X, LaVision GmbH) and image acquisition was performed using DaVis 8.4 software (LaVision GmbH).The fluids within the flume were seeded with 2 µm silver coated hollow glass spheres (SG02S40, Potters Industries).The number density of tracers within the images was approximately 0.05 particles per pixels.For the Newtonian and non-Newtonian flows, eight datasets, equivalent to 114 832 images, were collected to ensure sufficient convergence of the different ensemble statistics in the analysis.One time-resolved dataset, for both measurements of the Newtonian and non-Newtonian TBLs, consisted of 14 354 single-frame images captured at a selected frequency between 0.52 kHz and 1.82 kHz.Therefore, one dataset took between 7.9 s and 27.6 s.This is equivalent to 36.2T and 62.7T, where T = δ/U ∞ is a representative advection time or large eddy turnover time and δ is the boundary layer thickness.The total duration of the eight datasets used for computing ensemble statistics was between 260T to 500T depending on the flow condition.The frequency was selected depending on U ∞ , and such that a maximum particle displacement of 5 pixels across subsequent images was achieved.Image processing consisted of first determining the minimum intensity of each pixel over the complete image ensemble, and then subtracting the minimum from all images in a dataset.Second, the intensity signal at each pixel was normalized by the average intensity of the ensemble.Lastly, a moving local minimum was calculated and subtracted within a kernel size of 5 pixels and local intensity normalization with a kernel size of 500 pixels were applied to every image.The statistical convergence for the mean velocity and Reynolds stresses of the Newtonian and non-Newtonian boundary layers were confirmed.All velocity statistics attain sufficient statistical convergence, with low random errors (less than 3.3 %), within the last 5700 realizations.
Calibration of the imaging set-up was achieved by fitting a third-order polynomial mapping function onto images of a dual-plane 3-D calibration target (025-3.3,LaVision GmbH).Volume self-calibration was used to significantly improve the accuracy of the mapping function (Wieneke 2008).Self-calibration reduced the average and maximum disparity vector magnitude, or error in the mapping function, to 0.02 and 0.06 pixels, respectively.After self-calibration, an optical transfer function was generated to account for changes in the imaged particle patterns across the 3-D volume (Schanz et al. 2013).The resulting VOI had dimensions ( x, y, z) = (272, 1220, 102) voxel = (8.0,35.8, 3.0) mm 3 , as shown in figure 4(b).Finally, the STB algorithm was performed using DaVis 10.2 software (LaVision GmbH).The maximum triangulation error was set to 1 voxel, and particle displacements were limited to a maximum of 8 voxel.Particles with an acceleration that was larger than 2 pixels or 20 % between subsequent image frames were discarded.The STB algorithm yielded approximately 6200 Lagrangian trajectories per time step within the VOI.
Once the Eulerian vector field is obtained, a moving first-order polynomial with a length of nine time steps was fit on the particle trajectories.Two types of binning were used to convert the Lagrangian trajectories into Eulerian vector components.The first involved averaging the trajectories within slabs that were parallel with the wall and covered the entire measurement domain along x and z.Each slab was 6 voxels or 0.18 mm (1.3δ v − 1.8δ v ) thick in the y direction.Neighbouring slabs along y overlapped by 75 %.This binning procedure was used exclusively for establishing the mean streamwise velocity U with high spatial resolution.Here, the angle brackets • • • denote averaging in time and along the spatially homogeneous direction z.It was also assessed that U did not vary significantly along x within the VOI; hence, the statistics were also averaged along the x direction within the VOI.The second binning procedure involved averaging particle tracks for each time step in 32 × 32 × 32 voxel or 0.94 × 0.94 × 0.94 mm 3 cubes to obtain the instantaneous velocity vector U within the domain.Neighbouring cubes had 75 % overlap with one another along the three Cartesian directions.Therefore, adjacent vectors were separated by 8 voxels or 0.235 mm.In terms of viscous wall units δ v = ν/u τ , the bins were between 6.9δ v × 6.9δ v × 6.9δ v and 9.3δ v × 9.3δ v × 9.3δ v depending on the flow considered.Here, u τ is the friction velocity and ν is the kinematic viscosity.The streamwise, wall-normal and spanwise components of the instantaneous velocity U are denoted as U, V and W, respectively.Velocity fluctuations were represented using lower case symbols, i.e. u, v and w.
A moving first-order polynomial function was fitted to the velocity components at each instance of time and then differentiated to obtain spatial gradients in velocity.The size or extent of the polynomial function was three velocity vector components along each Cartesian direction, which equates to 24 × 24 × 24 voxels or 0.70 × 0.70 × 0.70 mm 3 .Spatial velocity gradients were then used to compute the topology parameters of the Newtonian and non-Newtonian TBLs according to § 2.
The uncertainty in the 3-D-PTV measurements is scrutinized in Appendix B. Uncertainty is primarily assessed based on how well the velocity vectors satisfy the divergence-free condition, where ∇ • U = 0. Appendix B demonstrates that the present measurements adequately satisfy the divergence-free condition compared with other investigations that have utilized experimental flow measurements to measure the VGT (Tsinober, Kit & Dracos 1992 The variables for inner scaling were established by fitting a linear function to the mean velocity profile U of each flow near the wall.The linear function was then differentiated in order to determine the near-wall shear rate γw of each flow.Here, γw is established by differentiating the mean velocity, i.e. d U /dy, for y > 0.2 mm and y + < 3. The lower bound of the fit was the smallest measurable value of y with a slab that did not overlap with the wall.While the upper bound of the fit is within the theoretical limit of the linear viscous sublayer.The wall shear stress τ w was then established according to τ w = η( γw ) γw , where η( γw ) is the viscosity of the fluid evaluated at the near-wall shear rate γw using the Carreau model that was fitted to measured values of η for PAM detailed in Appendix A. After establishing τ w , the friction velocity u 2 τ = τ w /ρ and wall units δ v = ν/u τ were determined, where ν = η( γw )/ρ is the near-wall kinematic viscosity and ρ is the fluid density.Variables normalized by inner scaling were denoted using the superscript +, where velocity statistics were normalized by u τ and position values were normalized by δ v .Several other variables were also used to characterize the flows.For example, the skin-friction coefficient C f = 2τ w /ρU 2 ∞ was used to defined the local friction of the boundary layer.The friction Reynolds number Re τ = δ/δ v defined as the ratio between the boundary layer thickness δ and the viscous wall units.Lastly, the Weissenberg number Wi = t e γw was used to the define the ratio between the elastic and viscous forces of the flow.The corresponding variables of the flow are listed in table 1.

Planar PIV
For all of the flows considered, the VOI measured using 3-D-PTV did not capture the complete boundary layer thickness along y.Therefore, a planar PIV set-up was used to obtain measurements of U over a larger field of view exceeding δ, in order to determine the bulk flow properties or outer scaling variables of the Newtonian and non-Newtonian TBLs.These bulk properties include the momentum thickness θ, boundary layer thickness δ and free-stream velocity U ∞ , all of which are listed in table 1.
The planar PIV set-up consisted of two double-frame digital cameras (Imager Intense, LaVision GmbH), each of which had a 1376 × 1040 pixels charged-coupled device sensor.Each pixel in the sensor was 6.45 × 6.45 µm 2 in size and had a 12 bit digital resolution.The sensors were cropped to 1376 × 128 pixels to enable higher acquisition rates, where the 1376 pixel dimension was parallel to the y direction.Double-frame images were acquired at a frequency of 14.3 Hz.The fields of view (FOVs) of both cameras were stacked along the wall-normal direction y, and covered a region with a size of x = 7.0 mm and y = 143.1 mm.The FOVs were placed at the centre of the channel along z and 200 mm upstream of the 3-D-PTV measurement location, along x.Illumination was provided from a 15 mJ pulse −1 Nd:YAG laser (Solo I-15, New Wave Research Inc.) that was synchronized with the cameras using a programmable timing unit (PTU 9, LaVision GmbH) and DaVis 7.3 software (LaVision GmbH).Two spherical lenses (one concave, the other convex) and one concave cylindrical lens expanded the laser beam into a 20-mm-wide (along x) and a 1-mm-thick (along z) laser sheet.One dataset consisted of 800 pairs of double-frame images, which took 56 s to collect.The time delay t between laser pulses of each image pair was between 1.43 and 5.00 ms depending on U ∞ .The value of t was chosen such that the maximum particle displacement between image frames was approximately 15 pixels.Recall from § 3 that eight datasets were collected for the two cases of water (corresponding to different Re θ ) and the one condition of PAM.Therefore, each flow scenario consisted of 6400 double-frame images.
Image processing was performed using DaVis 8.4 software (LaVision GmbH).First the minimum intensity in each pixel was determined in each dataset and subtracted from every image in the ensemble.Second, the intensity signals in each pixel were normalized by the average intensity of the ensemble.Velocity vectors were then established using cross-correlation with an initial interrogation window (IW) size of 64 × 64 pixels and a final IW size of 24 × 24 pixels with 75 % overlap between neighbouring IWs.The mean streamwise velocity U with respect to y was determined by averaging U over all instances of time t and along the x direction.Profiles of U with respect to y were then used to identify the free-stream velocity U ∞ , the boundary layer thickness δ and momentum thickness θ as listed in table 1.The boundary layer thickness is assessed as the y location where U = 0.99U ∞ .The Reynolds number based on the momentum thickness is defined as Re θ = U ∞ θ/ν (recall that ν = η( γw )/ρ, where η( γw ) is assessed at the given near-wall shear rate).A local DR percentage DR for the polymer-laden TBL was defined according to where C f ,p is the skin friction of the polymer-laden boundary layer and C f ,n is the skin-friction coefficient of the Newtonian boundary layer at a similar Re θ .Comparing the C f values in rows 2 and 3 of table 1 demonstrates that the PAM flow has a DR of 33.1 %.

Results and discussion
Results of the 3-D flow measurements involving the Newtonian and polymer-laden boundary layers are presented in two parts.First, more conventional ensemble statistics such as mean velocity profiles, Reynolds stresses and two-point velocity correlations are presented.After which, the Δ-criterion is used to comment on the topology of each flow.30, a feature common in drag-reduced flows of polymer solutions.The intercept B of the polymer-laden boundary layer is larger than B for water, and visually κ is approximately the same.Although U + is enhanced within the outer layer of the polymer-laden flow, it does not overlap with the maximum DR asymptote U + = 11.7 ln( y + ) − 17.0 of Virk, Mickley & Smith (1970).

Velocity statistics
Figure 5(b) shows inner-normalized plots of the four non-zero components of the Reynolds stress tensor with respect to y + .In descending order of magnitude, u 2 + , w 2 + and v 2 + are the streamwise, spanwise and wall-normal Reynolds stresses, respectively, and uv + is the Reynolds shear stress.The experimentally measured profiles of u 2 + , v 2 + and uv + for water overlap well with the DNS of Jiménez et al. (2010) at a comparable Re θ .However, the measured Reynolds stress profiles of w 2 + for water are marginally less than that of the Newtonian DNS.That being said, profiles of w 2 + for water with slightly different Re θ only show a subtle difference and are rather consistent with one another.The discrepancy among DNS and the measured profiles of w 2 + is attributed to experimental uncertainties (discussed in Appendix B).Measurements of the out-of-plane velocity component, in this case W, are generally more erroneous using 3-D-PTV, hence, errors in w 2 + are more expected (Warwaruk & Ghaemi 2021).Overall, the polymer-laden boundary layer has augmented values of u 2 + for y + < 150 and attenuated values of w 2 + , v 2 + and − uv + for y + < 100, when compared with the boundary layers of water.The peak in u 2 + is also shifted away from the wall for the PAM flow relative to water; for PAM, the peak in u 2 + is at a y + of 21, while for both of the water flows, the peak in u 2 + is at a y + of approximately 13.
Experimentally measured mean velocity and Reynolds stress profiles of PAM, shown in figure 5, reflect consistency with prior measurements of polymer drag-reduced flows with low drag reduction (LDR) percentages that are less than 38 % (Warholic, Massah & Hanratty 1999).Low drag reduction flows typically have an expanded buffer layer and a log layer with a larger B -often referred to as a Newtonian plug (Virk et al. 1970;Warholic et al. 1999).The larger B is visually apparent in figure 5(a), and the expanded buffer layer is evident based on the shift in the peak of u 2 + to larger y + , seen in figure 5(b).Warholic et al. (1999) similarly demonstrated that polymer drag-reduced channel flows at LDR consist of augmented u 2 + values and attenuated w 2 + , v 2 + and − uv + values relative to water at a comparable Re.Generally, the ensemble velocity statistics of PAM are in good agreement with the LDR flows depicted in Warholic et al. (1999) and other investigations (Escudier, Nickson & Poole 2009;Warwaruk & Ghaemi 2022;Mitishita, Elfring & Frigaard 2023).
Two-point correlation of the streamwise velocity fluctuations u is used to obtain a depiction of the integral length scale within the buffer layer of each flow.Moreover, it is the most common metric used in prior investigations of polymer drag-reduced flows for quantifying the size of large-scale turbulent motions.Therefore, it provides another good baseline comparison between the current and prior investigations of LDR flows.The spatial two-point correlation is calculated according to where (x + 0 , y + 0 , z + 0 ) is the coordinate of a reference point, and (δx + , δy + , δz + ) are small displacements relative to the point of reference.Here, the point of reference is taken to be (x + 0 , y + 0 , z + 0 ) = (0, 20, 0), which is at the border of the domain along x and z, and in the buffer layer of the flow along y.
Open contours of C uu along the xy plane and at z + = 0 are shown in figure 6(a).Contours are coloured according to the different flows and similar to that of figure 5.For the water flows at different Re θ , contours of C uu approximately overlap, implying that the length of the large-scale motions in viscous wall units are the same.Evidently, the VOI is not large enough along x to capture the complete integral length scale of each flow, or where C uu becomes zero.That being said, it is clear that the PAM flow has a different distribution of C uu than water.Compare, for example, C uu with a value 0.95 or 0.85 in figure 6(a) for PAM to water.Values of C uu = 0.95 for water extend to (δx + , δy + ) = (23.0,4.8) while for PAM, values of C uu = 0.95 stretch to (δx + , δy + ) = (42.3,2.8).This demonstrates that the large-scale motions within the buffer layer of the PAM boundary layer are double the length along x compared with those of water, and less angled upwards along y.
Contours of C uu along the xz plane and at y + = 20 can be seen in figure 6(b).Similar to the xy plane, contours of C uu along the xz plane overlap for the water flows with different Re θ , implying that the size of the large-scale motions in viscous wall units are the same.Based on figure 6(b) it is also apparent that the VOI is not wide enough along z to capture the complete spanwise width of the large-scale motions where C uu = 0.However, much like figure 6(a), there is an unambiguous difference in the contours of C uu along the xz plane among PAM and water.Contours of C uu that are similar in value extend to larger δ + z for PAM compared with water.For example, when δ + x = 0, values of C uu equal to 0.85 extend to δ + z of 10.6 for water.For PAM, the contour of C uu = 0.85 extends farther, to δ + z of 17.6, implying that the large-scale motions in the flow of PAM are wider compared with water.As alluded to in § 1, an elongation and widening of high-and low-speed velocity streaks is a common feature of polymer drag-reduced flows (Warholic et al. 1999;White et al. 2004;Farsiani et al. 2020;Warwaruk & Ghaemi 2021).The difference in C uu among PAM and water observed in figure 6 implies the same augmentation to size of the large-scale flow motions within the buffer layer.
Overall, the results of the current section demonstrate that the PAM boundary layer has one-point and two-point turbulent statistics common for an LDR flow.It does not, however, provide a complete depiction of how, and why, the velocity statistics within the polymer-laden flow are different than a Newtonian TBL.For this, the distribution of fine-scale motions and streamline patterns within the Newtonian and non-Newtonian boundary layers are scrutinized using the Δ-criterion.

Probability density function of invariants
The topology of the Newtonian and non-Newtonian boundary layer is evaluated using the Δ-criterion detailed in § 2. Previous investigations of wall-bounded turbulence generally separate the topology of the flows into different regions of y + , e.g.viscous sublayer, buffer layer, log layer and wake region.Before separating the flow into these different wall-normal regions, the invariants in L, D and W are evaluated for the complete spatial domain.Note that all gradients are made dimensionless by multiplying the components of L by the large eddy turnover time T = δ/U ∞ of each flow.Probability density functions (p.d.f.s) are normalized histograms of all non-zero invariants Q, R, Q D , Q W and R D , as well as the discriminant in (2.1) Δ and (2.4) Δ D .As discussed in § 2, if the flow is assumed to be incompressible, the first invariant of L should be zero, i.e.P = 0.However, divergence errors inherent in many experimental measurements produce finite values of P. Therefore, p.d.f.s of P are also shown for comparison.
The p.d.f.s of P, Q and R are shown in figure 7(a) for the boundary layers of water at Re θ = 1814 and 2257, and PAM.The p.d.f.s of P are shown with solid lines, Q with dashed lines and R with dotted lines.The finite values of P are due to a divergence error caused by experimental noise and the limited spatial resolution involved with binning the Lagrangian trajectories produced from 3-D-PTV.This error has been shown to impact the measured topology of each flow using the Δ-criterion (Ganapathisubramani et al. 2007; The p.d.f. in R also covers a larger range of values than Q.Relative to water, the range in possible values of both Q and R is narrower in the PAM flow; however, the attenuation in R appears to be larger than that of Q.A more narrow range in Q implies that both vortical and dissipative flow motions are in less abundance within the PAM flow.An attenuation in the range of R demonstrates that the PAM flow experiences fewer instances of fluid extension and compression.A similar reduction in the range of R was observed by Mortimer & Fairweather (2022) in their drag-reduced channel flow DNS using the FENE-P constitutive model.Interestingly, p.d.f.s of Q and R for PAM do not have a noticeable skeweness and reflect a similar range of values, unlike the p.d.f.s for water.
Figure 7(b) shows the p.d.f.s of Q W with dashed lines, Q D with solid lines and R D with dotted lines, for the flows of water and PAM.As expected, all values of Q D are negative, while all values of Q W are positive.Similar to figure 7(a), p.d.f.s of Q W , Q D and R D overlap for the flows of water at different Re θ .The p.d.f.s of R D are more positively skewed, implying the straining flow motions are more compressive (unstable) than stretching (stable).Compared with the water flows, the PAM flow has a higher likelihood of non-zero values of Q W and Q D compared with water -an opposite trend than the p.d.f.s shown in figure 7(a).The p.d.f. of R D is similar for PAM and water for negative values of R D ; however, the probability of positive R D values is lower for PAM compared with water.Therefore, the PAM flows exhibit fewer compressive or biaxial straining motions compared with water, given the lower p.d.f.values of positive R D .
Figure 7(c) shows p.d.f.s of the discriminant Δ established using (2.3).The p.d.f.s of Δ are positively skewed and overlap for the two boundary layer flows of water.The positive skewness shows that more flow motions are focal than dissipative in the Newtonian boundary layers.The boundary layer flow of PAM, on the other hand, has overall fewer instances of non-zero Δ.These reinforce the observation of figure 7(a) -namely that PAM has a lower amount of both focal and dissipative flow motions.The p.d.f.s of Δ D determined from (2.6) are provided in figure 7(d).Recall from § 2 that the discriminant Δ D should be less than 0 for an incompressible flow.In other words, this is predicated on the assumption that P = P D = 0 and the notion that (2.6)only consists of the invariants Q D and R D .Therefore, the positive values of Δ D seen in the p.d.f.s of figure 7(d) are a result of the divergence error or non-zero values of P. Despite the appearance that the PAM flow has fewer instances of Δ D > 0 in figure 7(d), the percentage of values with Δ D > 0 among all flows is similar and between 12-13 %.Although this is not ideal, this discrepancy is not outside the norm for experimentally derived velocity vectors -see the comparable divergence error among the current measurements and previous experimental works in Appendix B.

Flow topology of the Newtonian flows
The j.p.d.f.s of the different invariants in L, D and W are used to determine the topology of flow motions within the buffer layer (5 < y + < 30), the log layer (y + > 30, y/δ < 0.3) and the wake region (y/δ > 0.3).The j.p.d.f.s of Q and R (similar to figure 1), Q D and R D (figure 2), −Q D and Q W (figure 3) are presented for each wall-normal region of the flow in the three rows of figure 8.The j.p.d.f.s of the different tensor invariants for water with an Re θ of 1814, alongside the other flow of water with an Re θ of 2257, are presented using filled contours and the open contours with black dashed lines, respectively.The j.p.d.f. of Q and R within the buffer layer, log layer and wake region are seen in figures 8(a-c), respectively.Within the buffer layer, i.e. figure 8(a), the Q − R j.p.d.f. is skewed towards positive Q, but rather evenly distributed among positive and negative values of R. Overall, there is preference towards focal topologies with Δ > 0. Moving -60 -30 30  farther away from the wall and into the log layer, the Q − R j.p.d.f. in figure 8(b) continues to reflect a preference for topologies with Δ > 0. As expected, the strength of the velocity gradients diminishes with increasing distance from the wall and the range of possible Q and R values decreases, i.e. the pattern shrinks.Within the log layer, the shape of the Q − R j.p.d.f.takes on a more well-defined tear-drop pattern with a clear point at the right-Vieillefosse tail (Δ = 0, R > 0) compared with the j.p.d.f. of the buffer layer in figure 8(a).Moving into the wake region, figure 8(c) shows that the range in possible values of Q and R continues to decrease with increasing y.That being said, the general shape of the Q − R j.p.d.f. is similar to that of the log layer in figure 8(b).A similar enhancement in the shape of the tear-drop pattern with increasing y was also observed in Newtonian DNS of channel flows by both Blackburn et al. (1996) with an Re τ of 395 and Mortimer & Fairweather (2022) with an Re τ of 180, as well as boundary layers by Chong et al. (1998), who used the boundary layer DNS of Spalart (1988) with an Re θ of 670.When comparing the j.p.d.f.s of Q and R for water at different Re θ , similar contour levels overlap within their respective wall-normal region of the flow, implying the flows at different Re θ posses a similar distribution of fine-scale motions.
The most notable difference between the Q − R j.p.d.f.s of figure 8(a-c) and that of Newtonian wall-bounded DNS (Blackburn et al. 1996;Chong et al. 1998;Mortimer & Fairweather 2022) is that DNS produces a more 'pointed' ridge at the right-Vieillefosse tail.Buxton et al. (2011) demonstrated that divergence errors, inherent in most experimentally derived velocity vectors, do not alter the general shape and limits of the Q − R j.p.d.f., with the exception that it erodes the tip of the Q − R j.p.d.f.along the right-Vieillefosse tail, making it more rounded.Although the tip of the tear-drop pattern becomes more rounded from divergence errors, Buxton et al. (2011) demonstrated that it continues to remain centred on the right-Vieillefosse tail, i.e.Δ = 0. Considering the present measurements have a comparable divergence error to that of prior experimental investigations of the VGT, as demonstrated in Appendix B, the j.p.d.f.s shown in figure 8(a-c) should provide a reasonable depiction of the distribution of fine-scale motions within the Newtonian boundary layer.Also, the j.p.d.f.s of Q and R take on a similar shape as those derived experimentally in the log layer of a Newtonian TBL (Elsinga & Marusic 2010).
Figure 8(df ) shows the j.p.d.f.s of the invariants in D for the water boundary layers with different Re θ .The j.p.d.f.s of Q D and R D are presented alongside lines of different eigenvalue ratios, namely Γ 2 /Γ 1 , as shown in figure 8( f ).Recall from § 2 that Γ 2 /Γ 1 = 1 corresponds to biaxial extension, Γ 2 /Γ 1 = 0 represents steady shear or planar extension, and Γ 2 /Γ 1 = −1/2 is uniaxial extension.Ashurst et al. (1987) demonstrated that the most probable eigenvalue ratio was Γ 2 /Γ 1 of 1/3 using DNS of Newtonian isotropic turbulence, hence, Γ 2 /Γ 1 = 1/3 is also shown on figure 8(df ).Within the buffer layer, shown in figure 8(d), there is a higher preference towards more biaxial extensional flow motions with R D > 0 and Γ 2 /Γ 1 between 0 and 1.Interestingly, a large ridge in the j.p.d.f. in the buffer layer appears to align with the preferential eigenvalue ratio of Γ 2 /Γ 1 = 1/3 for the Newtonian isotropic turbulence found by Ashurst et al. (1987).Moving away from the wall to the log layer and wake region shown in figure 8(e, f ), the flow becomes increasingly skewed toward biaxial extensional flow events (R D > 0 and 0 < Γ 2 /Γ 1 < 1).Compared with the j.p.d.f. of the buffer layer, shown in figure 8(d), the log layer and wake regions have more events with Δ D > 0, indicative of divergence errors.Based on Appendix B, and also shown in Ganapathisubramani et al. (2007) and Gomes-Fernandes et al. (2014), regions of the flow with lower velocity gradients are generally coupled with larger divergence errors.Therefore, it is expected that the log and wake layers, with overall smaller velocity gradients than the buffer layer, may exhibit higher divergence errorsan effect of this being a positive Δ D .That being said, the j.p.d.f.s of Q D and R D are generally similar to those derived from Blackburn et al. (1996) and Chong et al. (1998) using DNS of a Newtonian channel flows (Re τ = 395) and boundary layers (Re θ = 670), where preference to R D > 0 grows as y increases.Similar to the VGT invariants, j.p.d.f.s of Q D − R D for water at different Re θ overlap, implying the straining motions are similar among the two Newtonian TBLs with a slightly different Re θ .
The j.p.f.s of the invariants −Q D and Q W are presented for the water boundary layers in figure 8(g-i), similar to that of figure 3. Much like the previously detailed j.p.d.f.s, the j.p.d.f.s of −Q D and Q W overlap for the water flows at the two Re θ .Within the buffer layer of the flow, shown in figure 8(g), there is a preference towards flow motions exhibiting conditions consistent with steady shear, with K = 1.Soria et al. (1994) detailed that turbulent mixing layers with flow regions having K = 1 consisted almost entirely of vortex sheets.Chong et al. (1998) demonstrated a similar preference to K = 1 and shear-dominant topologies within the buffer layer of a turbulent boundary flow with an Re θ of 670, that was derived from Newtonian DNS (Spalart 1988).Although the j.p.d.f. of figure 8(g) is concentrated around K = 1, there are deviations, particularly at smaller values of −Q D and Q W . Chong et al. (1998) similarly observed subtle deviations from K = 1 within the buffer layer near the origin of −Q D and Q W in their analysis of Newtonian boundary flow DNS by Spalart (1988).Within the log and wake layers of the flow, shown in figure 8(h,i), a large spread between K of 0 and ∞ emerges.Therefore, fine-scale motions within the log and wake layers take on a variety of patterns, ranging from extensional to rotational.Topology in figure 8(h,i) is similar to isotropic turbulence seen in Ooi et al. (1999).

Flow topology of the polymer-laden flow
The j.p.d.f.s of the invariants of L, D and W are shown in figure 9 for the polymer-laden boundary layer at different wall-normal regions of the flow.The limits of the wall-normal regions are the same as those from figure 8. Open contours with black dashed lines in figure 9 are the j.p.d.f.s of water with an Re θ of 2257 while the filled contours are the j.p.d.f.s of PAM at Re θ = 2290.Figure 9(a) provides the j.p.d.f. of Q and R for 5 < y + < 30.Compared with the flow of water at a similar Re θ , the PAM boundary layer has attenuated values of Q and R. The range in possible R values narrows considerably compared with water -almost a two-fold reduction in the largest magnitude of R. A narrower range in R was similarly observed by Mortimer & Fairweather (2022) for drag-reduced viscoelastic channel flows at an Re τ of 180 and derived from DNS.This is a general indication that stretching and extensional motions within the flow are diminished.Furthermore, the narrowing of Q demonstrates that strong vortical and dissipative motions are less common.Moving away from the wall, figure 9(b) shows the Q − R j.p.d.f. for y + > 30 and y/δ < 0.3.Evidently, a reduction in the magnitude of Q and R relative to water at a similar Re θ is still present farther from the wall.The tear-drop pattern no longer exists in the Q − R j.p.d.f. of PAM, and a well-defined tip does not appear along the right-Vieillefosse tail.The trend continues into the wake region of the flow; figure 9(c) again shows how the range of possible Q and R values is diminished for PAM relative to water.This is despite the fact that the boundary layers of PAM and water have comparable velocity fluctuations within the outer layer of the flow, as seen in figure 5(b).
In viscoelastic simulations of a low-Reynolds-number transitional channel flow exhibiting EIT, Dubief et al. (2013) demonstrated that j.p.d.f.s of Q and R exhibited an oval pattern, that was more narrow along R than Q.The oval pattern was also relatively symmetric about Q = 0 and R = 0.The narrowing of R, seen in figure 9(a-c), is perhaps indicative that the polymer-laden flow is exhibiting dynamics more akin to EIT.That said, the topology of the polymer-laden flow is not identical to EIT; the j.p.d.f.s of Q and R seen in figure 9(a-c) are still asymmetric with respect to the axes of Q = 0 and R = 0.However, the possibility that EIT exists within the polymer-laden boundary layer is not yet ruled out.Observations of instantaneous flow structures have not been made, and it is possible that EIT might exist in some capacity within the flow.
Perhaps the most obvious difference between the topology of PAM and water are revealed in the j.p.d.f.s of Q D and R D . Figure 9(d) shows the Q D − R D j.p.d.f. for the polymer-laden boundary layer relative to water for 5 < y + < 30.Although there is still a bias towards biaxial extensional flow motions, the preference to R D > 0 is greatly -60 -30 30  diminished relative to water at a similar Re θ .Rather, the flow tends towards an eigenvalue ratio Γ 2 /Γ 1 of 0, where the flow is more two dimensional with conditions comparable to steady shear or planar extension.Farther from the wall for y + > 30, straining motions within the flow of PAM shown in figure 9(e, f ) become more biased towards biaxial stretching, but do not show as strong of a preference to Γ 2 /Γ 1 = 1 as seen for water.
The j.p.d.f.s of −Q D and Q W also demonstrate an unambiguous difference between fine-scale motions within the polymer-laden and Newtonian boundary layers.Compared with water, the flow of PAM near the wall shown in figure 9(g) consists of −Q D and Q W values that are almost always equivalent and concentrated on the line K = 1.Together, with figure 9(d), this implies that the near-wall flow of PAM is primarily two (1998) demonstrated that similar 2-D shear-dominant flow can also be found in Newtonian wall turbulence, albeit much closer to the wall and within the viscous sublayer (y + < 5).This could be indicative of an expansion in the thickness of the viscous sublayer of the polymer-laden flow.Moving farther from the wall and into the range of y + > 30 and y/δ < 0.3, the higher tendency for the PAM flow to exhibit features with K = 1 continues.
Compared with the flow of water at a similar Re θ , the j.p.d.f. of −Q D and Q W shown in figure 9(h) shows more of a preference towards shear-dominant flow with K = 1, albeit less so than the PAM flow near the wall for 5 < y + < 30.Within the wake region, figure 9(i) shows a more scattered j.p.d.f. of −Q D and Q W for the flow of PAM with no clear preference to a particular value of K, but also no overlap with the j.p.d.f. of water at a similar Re θ .
Based on the j.p.d.f.s of Q D and R D shown in figure 8(df ), most straining motions within the Newtonian boundary layers were closer to biaxial stretching, where Γ 2 /Γ 1 = 1.However, for the polymer-laden boundary layer, shown in figure 9(df ), straining motions near the wall were closer to the 2-D line where Γ 2 /Γ 1 = 0, and the local fine-scale motions are akin to steady shear or planar extension.The p.d.f.s of Γ 2 /Γ 1 are provided for the Newtonian and polymer-laden boundary layers within the buffer, log and wake regions in figure 10(a-c), respectively.The eigenvalues Γ 1 and Γ 2 are determined from locally solving (2.4) at every spatial coordinate and time instance.For the water flows, p.d.f.s of Γ 2 /Γ 1 overlap within the buffer layer, log layer and wake region.The probabilities of Γ 2 /Γ 1 > 0 for water are 58 %, 70 % and 70 % in the buffer layer, log layer and wake region, respectively, demonstrating the overall preference to a biaxial stretching topology.Based on the near-wall p.d.f. of Γ 2 /Γ 1 for the PAM boundary layer, shown in figure 10(a), there is a much higher probability of Γ 2 /Γ 1 being zero compared with the flows of water.Moreover, the Γ 2 /Γ 1 p.d.f. of the near-wall boundary layer of PAM, depicted in figure 10(a), has a probability of Γ 2 /Γ 1 > 0 of 49 %, which is 9 % lower than water.Therefore, biaxial stretching events with Γ 2 /Γ 1 > 0 are less abundant and 2-D shear or planar extensional flow features with Γ 2 /Γ 1 = 0 are more common in the polymer-laden boundary layers for y + < 30.Despite the appearance of subtle difference in the j.p.d.f.s of Q D and R D in the log and wake regions among PAM and water in figure 9(e, f ), the p.d.f.s of Γ 2 /Γ 1 shown in figure 10(b,c) demonstrate that the distribution of Γ 2 /Γ 1 values is similar for the Newtonian and polymer-laden flows.
The j.p.d.f.s of −Q D and Q W for the Newtonian boundary layers, shown in figure 8(g), demonstrated that the flow near the wall consisted mostly of 2-D shear layers where K = 1.However, in the log and wake layers, shown in figure 8(h,i), the flow had a variety of dissipative and vortical motions with K between 0 and ∞, similar to isotropic turbulence (Ooi et al. 1999).For the polymer-laden boundary layer, the flow was even more concentrated around K = 1 within the buffer and log layers in figure 9(g,h) compared with water, while the topology within the wake region was scattered, with K between 0 and ∞.The p.d.f.s of K for the Newtonian and polymer-laden boundary layers are shown for the buffer, log and wake regions of the flows in figure 10(df ).The p.d.f.s of K overlap for the flows of water at different Re θ at all wall-normal regions.Within the buffer layer, figure 10(d) shows visibly narrow Gaussian p.d.f.s of K where the average of K for water and the flow of PAM are both 1.However, the standard deviation in K for the polymer-laden flow is smaller and approximately equal to 0.15, compared with water where the standard deviation in K is 0.45.Within the log layer, water is slightly more biased towards K < 1; the mode and median in the p.d.f. of K for water shown in figure 10(e) is 0.685 and 0.910, respectively.For the polymer-laden boundary layer, the mode and median in the p.d.f. of K within the log layer, shown in figure 10(e), is larger compared with water and equal to 0.945 and 0.975, respectively.Therefore, the polymer-laden flow has less likelihood to exhibit dissipative topologies compared with water.In the wake region the p.d.f.s of water boundary layers shown in figure 10( f ) are not significantly different than those of water in the log layer seen in figure 10(e).Also similar to the log layer, the wake region of the polymer-laden flow has a lower probability of exhibiting dissipative flow topologies and a higher preference towards K of 1.

Conditional flow structures
The topology of fine-scale motions within the boundary layers of PAM and water are unique, as shown by the j.p.d.f.s of the different tensor invariants in figure 9 and the p.d.f.s of Γ 2 /Γ 1 and K in figure 10.To provide a more visual depiction of the differences in the topologies of each flow, the following section demonstrates sample velocity fields for the Newtonian and polymer-laden boundary layers alongside contours of positive and negative regions of Δ, and the VGT invariants Q and R. Linear stochastic estimation (LSE) is then used to provide an average velocity field associated with large positive and negative instances of Δ within the flow that correspond to the dominant focal and dissipative topologies, respectively.
An instantaneous snapshot of u + and streamlines along an xy plane situated at z = 1.5 mm is shown in figure 11 (g,h,i, j), respectively.Here, a region of the flow that exhibits shear-dominant 2-D flow is emphasized, which was previously shown to be in larger abundance within the polymer-laden flow based on figures 9 and 10.The particular 2-D shear-dominant region is located at (x + , y + ) = (36, 35) and denoted using a red marker in figure 11( fj).This region has relatively parallel streamlines in figure 11( f ), which is characteristic of shear flow.Correspondingly, values of Δ and Q are largely negative around the region of the flow indicated by the red marker, as shown in figure 11(g-i).Values of R are also small in magnitude at (x + , y + ) = (36, 35) and approximately equal to zero, implying the flow is more two dimensional.This provides a visual depiction of the velocity field associated with the 2-D shear-dominant events found to be in greater abundance within the boundary layer of PAM.
Among most snapshots within the polymer-laden flow, there are no obvious indicators of EIT.Specifically, the flow does not exhibit the distinct alternating regions of positive and negative Q, or Δ, along the x direction seen in low-Reynolds-number viscoelastic channel flow simulations by Samanta et al. (2013) or Dubief et al. (2013).It is suspected that EIT has not yet established a significant presence within the LDR flow, and higher amounts of DR could demonstrate topologies more comparable to EIT.
In addition to providing instantaneous snapshots of the velocity field, LSE is used to approximate the average velocity field associated to an event E at a particular spatial location (x + 0 , y + 0 , z + 0 ) within the VOI (Christensen & Adrian 2001;Elsinga et al. 2010Elsinga et al. , 2012)).The event E(x + 0 , y + 0 , z + 0 ) can be chosen as any scalar quantity derived from the measured velocity (Christensen & Adrian 2001); in this case E is chosen to be the discriminant Δ, in order to highlight the velocity fields associated with the dominant focal and dissipative events.The conditionally averaged velocity is represented as , where (4.2a) The conditional velocity u + |E is a linear function of E(x + 0 , y + 0 , z + 0 , t), and the coefficient of the linear function, C uE , is a time-independent two-point correlation of the velocity fluctuations u + = (u + , v + , w + ) and E (Christensen & Adrian 2001).Because C uE of (4.2b) is independent of time, the magnitude of u + |E can be amplified or attenuated based on E(x + 0 , y + 0 , z + 0 , t 0 ), where t 0 is a particular time instance.In this case, E is taken to be Δ at (x + 0 , y + 0 ) = (27, 50) and z 0 = 1.5 mm, which is at the centre of the VOI along x and z and at the lower extent of the log layer along y.For simplicity, only the conditional streamwise velocity u + |Δ and wall-normal velocity v + |Δ is determined using (4.2) along a 2-D xy plane at z 0 = 1.5 mm for the boundary layers of water at an Re θ of 2257 and PAM at an Re θ of 2290.The LSE coefficient is calculated with Δ < 0 and Δ > 0 in (4.2b) separately, to isolate the conditional velocity field associated with the dominate dissipative and focal fine-scale motions at (x + 0 , y + 0 ) = (27, 50).The conditional streamwise and wall-normal velocities, given negative Δ, are denoted as u + |(Δ < 0) and v + |(Δ < 0) , respectively.Similarly, the conditional streamwise and wall-normal velocities, given positive Δ, are denoted as u + |(Δ > 0) and v + |(Δ > 0) .For the LSE given negative Δ, t 0 in (4.2a) is chosen to be the instance in which Δ is minimum.On the other hand, t 0 in (4.2a) for the LSE given positive Δ, is chosen to be the instance of maximum Δ.These amplify the LSE such that the magnitude of conditional velocities are comparable to those shown in figure 11(a, f ).In figure 12, 2-D streamlines based on the conditional streamwise and wall-normal velocities are overlaid on contours of the conditional streamwise velocity.
The conditional streamwise velocities u + |(Δ < 0) and u + |(Δ > 0) , overlaid with streamlines are shown in figures 12(a) and 12(b), respectively, for the flow of water at an Re θ of 2257.In figure 12(a) the conditional velocity field corresponding to large negative Δ demonstrates a noticeable saddle point that is marginally upstream of the reference point (δx + , δy + ) = (0, 0).The saddle point is situated at the intersection of a sweep (u > 0, v < 0), located at δy + > 25, and ejection (u > 0, v < 0), located at δx + > 0 and −25 < δy + < 0. Two spanwise vortical motions can be seen within the conditionally averaged flow, one directly below the saddle point region, and the other, above and downstream of the saddle point.In figure 12(b) the conditional velocity field corresponding to Δ > 0 demonstrates a large spanwise vortex approximately centred on the reference point.Above the vortex, at δy + > 0, is a large high-speed zone with u > 0, while below the vortex (δy + < 0) there is narrow low-speed zone with u < 0. Together, figures 12(a) and 12(b) produce a spatial velocity pattern similar to a hairpin packet dissected at its centre along the xy plane.Figure 12(a) shows the saddle point between two neighbouring hairpins along x, where the high-speed sweep of an upstream hairpin meets the low-speed ejection of another downstream hairpin vortex.Figure 12(b) shows the head of the hairpins, which consists of a large spanwise vortex.Therefore, the most dominant dissipative (Δ < 0) and focal (Δ > 0) events within a Newtonian TBL correspond to fine-scale motions that make up a hairpin packet.The former being a saddle point at the intersection of two neighbouring hairpins, the later being the hairpin heads.
The conditional velocity fields for the polymer-laden boundary layer with an Re θ of 2290 are shown in figures 12(c) and 12(d), for Δ < 0 and Δ > 0, respectively.The velocity fields are extracted based on the signal of Δ at the same reference point of (x + 0 , y + 0 ) = (27, 50), as that previously used for water in figure 12(a,b).The conditional velocity field corresponding to large negative Δ, shown in figure 12(c), demonstrates a low-speed zone or ejection event (u < 0, v > 0).The conditional velocity field associated with Δ > 0, shown in figure 12(d), consists of an upward-tilted high-speed zone or an outward interaction (u > 0, v > 0), in stark contrast to the low-speed zone seen in figure 12(c).Overall, the conditional flow fields of the polymeric boundary layer, shown in figure 12(c,d), do not exhibit the same hairpin structure implied from the conditional velocity field for water and shown in figure 12(a,b).Rather, conditional flow fields consist of low-and high-speed shear layers, where streamlines are approximately parallel with respect to the wall.These shear layers are consistent with the previous observations that the PAM boundary layer is more shear dominant, and consists of fewer biaxial and vortical motions near the wall.

Further discussion
In § 4 it was demonstrated that extensional straining motions, particularly those exhibiting biaxial extension with R D > 0 and 0 < Γ 2 /Γ 1 < 1, are less abundant within the buffer layer of the polymeric flow compared with water.This was shown by the more narrow range in R of figures 7(a) and 9(a), as well as the lower preference to straining motions with R D > 0 or 0 < Γ 2 /Γ 1 < 1 seen in figures 7(b), 9(d) and 10(a).Furthermore, figures 7(a) and 9(a) demonstrated that flow motions with a large magnitude in Q were less present in the polymeric flow relative to water, implying an attenuation in the strength of vorticity (Q > 0) and dissipation (Q < 0).Instead, figures 9(d) and 9(g), as well as figures 10(a) and 10(d), demonstrated that the polymer-laden flow had a higher preference to 2-D shear-dominant structures, with R D = 0, Γ 2 /Γ 1 = 0 and K = 1.These shear-dominant structures are similar to those seen in the viscous sublayer of Newtonian wall turbulence, as demonstrated by the boundary layer DNS of Chong et al. (1998) at an Re θ of 670 and channel flow DNS of Blackburn et al. (1996) at an Re τ of 395.The notable difference is that for the polymer-laden flow, these 2-D shear-dominant structures exist outside the conventional limits of the viscous sublayer (y + > 5), implying that the viscous sublayer of the polymer-laden flow is thicker compared with water.
The observation of a thicker viscous sublayer is consistent with the lower magnitude in the wall-normal Reynolds stress v 2 + and Reynolds shear stress uv + within the buffer layer of the polymer-laden flow compared with water, seen in figure 5(b) of § 3. The 2-D shear-dominant flow and expanded viscous sublayer agrees with the strong attenuation of wall-normal sweep and ejection motions commonly observed in drag-reduced viscoelastic DNS (Pereira et al. 2017) and experiments of polymer drag-reduced boundary layers (Shah et al. 2021).A suppression of sweep and ejection motions in the polymer-laden flow can also be reasonably implied from the current measurements based on the reduction in uv + shown in figure 5(b), as well as the stronger alignment between large-scale turbulent motions and the streamwise x direction shown in plots of the two-point correlation C uu in figure 6(a).The mechanism by which these sweep and ejection motions are suppressed appears to be an attenuation of the extensional flow motions where sweep and ejection events meet -an observation that was similarly implied in the polymer-laden boundary layer experiments of Shah et al. (2021).Conditionally averaged velocity fields for the Newtonian boundary layer, shown in figure 12(a,b), show that the dominant dissipative motion within the buffer layer is an extensional saddle point, located at the interface of a sweep and ejection.On the other hand, the same saddle point seen in the boundary layer of water is not present in the polymer-laden flow.Rather, the conditionally average velocity fields for the polymeric boundary layer, shown in figure 12(c,d), exhibit lowand high-speed zones with streamlines that are parallel with respect to the wall, consistent with the observation of more 2-D shear-dominant flow shown in figures 9 and 10.Classical theories regarding the mechanism of polymer DR, e.g. that proposed by Lumley (1973), assert that polymer drag-reduced flows typically have an expanded buffer layer relative to Newtonian wall-bounded turbulence due to an attenuation of the extensional motions within the flow.Our experimental results demonstrate that this assertion is plausible, given the fewer extensional flow motions near the wall and the expanded inner layer of the polymer-laden flow.

Conclusion
Prior works have asserted that the large extensional viscosity of polymer solutions opposes uniaxial and biaxial extensional flow regions, and mitigates the strength and formation of counter-rotating streamwise vortices (Lumley 1973;Roy et al. 2006).The present experimental investigation sought to observe this effect by measuring the distribution of extensional and vortical motions within a polymer-laden boundary layer using 3-D-PTV and the Δ-criterion of Chong et al. (1990).A polymer-laden boundary layer with Re τ = 687 and Re θ = 2290 was compared with two Newtonian TBLs, one at a similar friction Reynolds number Re τ of 612 and the other at a similar momentum thickness-based Reynolds number Re θ of 2257.Relative to the Newtonian boundary layer with a similar Re θ , the polymeric flow had a 33 % lower skin-friction coefficient.The j.p.d.f.s of the invariants in the VGT, the RDT and the RRT were used to establish a distribution of the different fine-scale motions within the polymer-laden and Newtonian boundary layers, some of which include extensional-and vortical-type flow motions.
Unambiguous difference in the j.p.d.f.s of the invariants in the VGT, Q and R, were observed between the polymer-laden and Newtonian boundary layers.The j.p.d.f.s of Q and R for the Newtonian boundary layers exhibited the well-known tear-drop shaped pattern with a clear ridge at the right-Vieillefosse tail.Relative to the Newtonian flows, the polymer-laden boundary layer had attenuated values of Q and R; although values of R were diminished much more than Q.A narrowing of R is the first evidence that uniaxial and biaxial stretching is less abundant within the polymer-laden flow.
Alterations to the invariants in the RDT and RRT are more telling of the attenuation of uniaxial and biaxial extension within the polymer-laden flow -particularly within the inner layer or y/δ < 0.3.Here, the invariants of the RDT, Q D and R D , imply that straining motions of the polymeric flow are more two dimensional considering there is a higher preference for the second eigenvalue in the RDT to be zero compared with water.Moreover, j.p.d.f.s of Q D and the invariant in the RRT Q W suggest that extensional flow motions (particularly biaxial extension) within the polymer-laden flow are less abundant and there is a larger preference towards shear-dominant flow motions.These shear-dominant structures are similar to those seen in the viscous sublayer of Newtonian turbulence.However, in the polymer-laden flow these structures are found at y + larger than the conventional limit of the viscous sublayer, implying that the viscous sublayer of the polymer-laden flow is thicker compared with water.
Overall, the notion that extensional flow motions are opposed within the polymer-laden boundary layer was confirmed using the measurements of the present work.It was demonstrated that biaxial extensional straining motions are less pervasive within the represent the range in the measurements of η at each γ .The error bars in η are slightly larger for the PAM solution than water (for M > 600 nN m and Ta < 1700) and can be attributed to some degradation in the samples as the fluids are pumped within the flume.The largest relative error in η is 4.9 %; therefore, despite slight amounts of degradation being present, its influence on the measurements of η are minimal.For a conservative estimate, it is assumed that the total uncertainty in measurements of η is the root sum of the squared systematic uncertainty, determined from the measurements of η for water, and the squared relative uncertainty of 4.9 % caused by degradation.In other words, the total relative uncertainty in η was taken to be 5.3 %.
The Carreau model was fit on the shear rheogram of the 140 ppm PAM solution to approximate the trend in η as a function of γ (Carreau 1972).The model was of the form where η 0 is the viscosity at γ = 0, η ∞ is the viscosity at γ = ∞, K is the consistency and m is the flow index.Nonlinear least square regression was used to fit (A1) onto the average values of η for the PAM solution between γ of 1 and 200 s −1 .The red solid line in figure 13 shows the Carreau model; the resulting fit of (A1) agrees well with the experimental measurements for PAM.The values of η 0 , η ∞ , K and m are 3.4 cP, 1.0 cP, 0.29 s and 0.76, respectively.

A.2. Extensional rheology
To evaluate the extensional rheology of water and the PAM solution, the deformation of a small droplet of fluid undergoing capillarly driven thinning was measured (Deblais et al. 2020;Rajesh et al. 2022).The droplet was generated by slowly extruding a small volume of fluid from a blunt-end nozzle with a diameter D 0 of 1.27 mm.A syringe pump ( Legacy 200,KD Scientific Inc.) was used to expel the droplet from the nozzle at a rate of 0.02 ml min −1 .Before the droplet detaches, a liquid bridge was formed between remnant fluid at the tip of the nozzle and the falling droplet.The rapid decay in the diameter of the liquid bridge D min was captured using a high-speed camera (NOVA S9, Photron Inc.) and back light illumination from a light-emitting diode.The high-speed camera had a 1024 × 1024 pixel complementary metal oxide semiconductor sensor with pixels that were 20 × 20 µm 2 in size and had a bit depth of 12 bit.The sensor was cropped to 896 × 512 to remove unused pixels in the image and increase the acquisition rate.A zoom lens was used to achieve a magnification of 4.3 and scale of 4.62 µm pixel −1 .For water, the thinning of the liquid bridge occurred rapidly, and images were acquired at 20 kHz.For the PAM solution, elastic forces prolonged the pinch-off process and an acquisition rate of 4 kHz was used.A similar configuration was used to measure the filament breakup of viscoelastic liquids in Deblais et al. (2020) and Rajesh et al. (2022).Three repeated measurements in the extensional rheometer were performed for water.Recall that eight samples of the PAM solution were collected immediately following 3-D-PTV data Three repeated measurements of the extensional rheology were performed for each sample of the PAM solution, resulting in 24 measurements in total.The minimum diameter D min of the liquid bridge was established using MATLAB software (Mathworks Inc.).For water, the liquid bridge ruptures quickly in t b of 25 ms due to inertial and capillary forces.The Ohnesorge number Oh = t v /t R relates the time scale associated with viscous forces t v = η 0 D 0 /2σ to that of surface tension and inertial forces, i.e. the Rayleigh time t R = (ρD 3 0 /8σ ) 1/2 .Here σ is the surface tension, which for water and low concentration solutions of PAM is generally 72 mNm −1 (Miller, Clasen & Rothstein 2009).For both water and PAM, Oh is less than 1, as shown in table 2, and the thinning process is dominated by inertial and capillary forces (Rajesh et al. 2022).However, for the PAM solution, elastic forces also contribute to the pinch-off dynamics.The Deborah number De = t e /t R represents the ratio of elastic forces to inertiocapillary forces, where t e is the elastic relaxation time of the fluid.When De is greater than 1, the droplet exhibits elastocapillary thinning described by where A = (GD 0 /2σ ) 1/3 and G is the elastic modulus of the fluid (Anna & McKinley 2001).Nonlinear least square regression is used to fit (A2) on the average measurements of D min /D 0 for t > t b of the PAM solution.The solid red line in figure 13(b) demonstrates to those seen in Ganapathisubramani et al. (2007) and Gomes-Fernandes et al. (2014).The divergence error, characterized by the horizontal spread in the j.p.d.f. of figure 15(b) along L ii /(L jk L jk ) 1/2 , is larger when (L jk L jk ) 1/2 T is lower for all flow conditions.Therefore, it is expected that velocity gradients that are lower in magnitude are more corrupted by divergence error than those with a higher magnitude, similar to the conclusion of Ganapathisubramani et al. (2007) and Gomes-Fernandes et al. (2014).

Figure 2 .
Figure 2. Ratios of eigenvalues for different R D and Q D for an incompressible flow with P = 0.The eigenvalues are listed in the descending order of Γ 1 : Γ 2 : Γ 3 (Blackburn et al. 1996).

Figure 3 .
Figure 3. Schematic of the different flow types in Q W , Q D space and for different kinematic vorticity numbers K (Soria et al. 1994).

Figure 4 .
Figure 4.A schematic of the 3-D-PTV flow measurement set-up with reference to a section of the water channel.Here (a) shows an isometric view of the measurement apparatus and water channel, (b) provides an isometric view of the VOI with reference to the Cartesian coordinate system, (c) shows a top view of the 3-D-PTV measurement set-up and (d) provides a front view of the measurement set-up.

Figure 5 .
Figure 5. Plots of the (a) mean velocity and (b) Reynolds stress profiles for the TBL flows of water and the 140 ppm PAM solution.The dotted lines are mean velocity and Reynolds stress profiles of the Newtonian TBL obtained from DNS of Jiménez et al. (2010) at Re θ = 1968.

Figure 6 .
Figure 6.Two-point correlation C uu of streamwise velocity fluctuations along the (a) xy plane at z + = 0 and (b) along the xz plane at y + = 20.The reference point for the correlation is (x + 0 , y + 0 , z + 0 ) = 0, 20, 0. The colours of the contours correspond to the same line colours and conditions of figure 5. Grey is water with Re θ = 1814, black is water with Re θ = 2257 and red is the 140 ppm PAM flow with Re θ = 2290.

Figure 8 .
Figure 8.The j.p.d.f.s of the invariants in the VGT, RDT and RRT for boundary layers of water.Rows of figure correspond to different wall-normal locations: (a-c) buffer layer, (df ) log layer, (g-i) wake region.Columns of figure correspond to j.p.d.f.s of different invariants: (a,d,g) Q and R, (b,e,h) Q D and R D , (c, f,i) −Q D and Q W . Filled contours are the j.p.d.f.s of water with Re θ = 1814, open contours with black dashed lines are the j.p.d.f.s of water with Re θ = 2257 at 10 −5 and 10 −4 .

Figure 9 .
Figure 9.The j.p.d.f.s of the invariants in the VGT, RDT and RRT for boundary layers of water.Rows of figure correspond to different wall-normal locations: (a-c) buffer layer, (df ) log layer, (g-i) wake region.Columns of figure correspond to j.p.d.f.s of different invariants: (a,d,g) Q and R, (b,e,h) Q D and R D , (c, f,i) −Q D and Q W . Filled contours are the j.p.d.f.s of the PAM boundary layer, open contours with black dashed lines are the j.p.d.f.s of water with Re θ = 2257 at 10 −5 and 10 −4 .

Figure 10 .
Figure10.Probability density functions of (a-c) the ratio between the second and first eigenvalues of D, and (df ) the kinematical vorticity number K from (2.8).The p.d.f.s in (a-c) are conditioned to exclude Δ D > 0. The p.d.f.s (a,d) correspond to the buffer layer, (b,e) the log layer and (c, f ) the wake region.
(a)  for the boundary layer of water at an Re θ of 2257.Corresponding contours of positive regions of Δ, negative regions of Δ, Q and R are 25

Figure 11 .
Figure 11.Instantaneous snapshots of u + (a, f ), positive Δ (b,g), negative Δ (c,h), Q (d,i) and R (e, j) for the boundary layer of water with an Re θ = 2257 and PAM.The upper row of figures (a-e) is the water flow, and the lower row ( fj) is PAM.The snapshots are shown along the xy plane at z = 1.5 mm, or the middle of the VOI.The blue dot indicates the spatial location (x + , y + ) = (18, 63), the magenta dot is (x + , y + ) = (45, 35) and the red dot is (x + , y + ) = (36, 35).Black lines in (a, f ) are streamlines.

Figure 12 .
Figure 12.Conditionally average velocity fields for the flow of water at an Re θ = 2257 (a) given Δ < 0 and (b) given Δ > 0; as well as the flow of PAM (a) given Δ < 0 and (d) Δ > 0. Velocity field is shown along the xy plane at z = 1.5 mm, or the middle of the VOI.All conditional averages are evaluated for (x + 0 , y + 0 ) = (27, 50).Filled contours are the streamwise velocity component of the conditionally averaged velocity, while black solid lines are streamlines.

Figure 13 .
Figure 13.Rheology measurements of tap water and the 140 ppm PAM solution.Here (a) corresponds to measurements of steady shear viscosity as a function of shear rate and (b) shows the diameter versus time of the thinning droplet expelled from a needle.Black dashed lines in (a) represent the lower and upper shear rate limits of the torsional rheometer.The solid red line in (a) is the fitted line of (A1) representative of the Carreau shear-thinning trend.The red solid line in (b) is the fitted line of (A2) that describes elastocapillary thinning.
Figure 13(b) shows the evolution of D min /D 0 with respect to time t.Here, the break-up time t b is subtracted from t on the horizontal axis.The markers in figure 13(b) represent the average values of the repeated measurements of D min for each instance of t.The sample error bars indicate the range in the repeated measurements of D min for each instance of t.

Table 1 .
Inner and outer scaling variables of the Newtonian and non-Newtonian TBLs.

Table 2 .
Time scales and dimensionless values for the droplet thinning process represented in figure 13(b) for water and PAM.