Monodisperse Double Emulsions Generated from a Microcapillary Device

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Science  22 Apr 2005:
Vol. 308, Issue 5721, pp. 537-541
DOI: 10.1126/science.1109164


Double emulsions are highly structured fluids consisting of emulsion drops that contain smaller droplets inside. Although double emulsions are potentially of commercial value, traditional fabrication by means of two emulsification steps leads to very ill-controlled structuring. Using a microcapillary device, we fabricated double emulsions that contained a single internal droplet in a core-shell geometry. We show that the droplet size can be quantitatively predicted from the flow profiles of the fluids. The double emulsions were used to generate encapsulation structures by manipulating the properties of the fluid that makes up the shell. The high degree of control afforded by this method and the completely separate fluid streams make this a flexible and promising technique.

Mixing two immiscible fluids produces an emulsion, which is defined as a dispersion of droplets of one fluid in a second fluid. Although they are not in equilibrium, emulsions can be metastable, with the droplets retaining their integrity for extended periods of time if their interface is stabilized by a surfactant. Emulsions play critical roles in many forms of processing and in coatings, foods, and cosmetics (1). One common use is to compartmentalize one fluid in a second, which is particularly important for packaging and stabilizing fluids and other active ingredients. Even more control and flexibility for encapsulation can be achieved through the use of double emulsions, which are emulsions with smaller droplets of a third fluid within the larger drops. The intermediate fluid adds an additional barrier that separates the innermost fluid from the outer fluid, or the continuous phase. This makes double emulsions highly desirable for applications in controlled release of substances (24); separation (5); and encapsulation of nutrients and flavors for food additives (68); and for the control of encapsulation, release, and rheology for personal care products (4, 911). Additional flexibility is achieved by controlling the state of the middle fluid, which can be selectively gelled or hardened to create solid capsules (12, 13). These capsules can be used to encapsulate of drugs for targeted delivery and release (1421).

Multiple emulsions are typically made in a two-step process, by first emulsifying the inner droplets in the middle fluid, and then undertaking a second emulsification step for the dispersion (22). Each emulsification step results in a highly polydisperse droplet distribution, exacerbating the polydispersity of the final double emulsion. Thus, any capsules formed from such double emulsions are, by nature, poorly controlled in both size and structure, and this limits their use in applications that require precise control and release of active materials. Microfluidic techniques can circumvent the vagaries of the bulk emulsification process and can produce more uniform double emulsions (23), although the range of drop sizes is limited and the devices require localized surface functionalization to control wettability in order to function. Alternatively, flow focusing of coaxial jets (24) can produce uniform coated droplets, but these must be reemulsified into the continuous phase, which is a difficult step that precludes widespread use of this technique. The availability of highly monodisperse double emulsions would not only greatly improve their applicability but would also allow for detailed studies of their stability under more controlled conditions (2531).

Here we describe a fluidic device that generates double emulsions in a single step, allowing precision control of the outer and inner drop sizes as well as the number of droplets encapsulated in each larger drop. Our device consists of cylindrical glass capillary tubes nested within a square glass tube. By ensuring that the outer diameter of the round tubes is the same as the inner dimension of the square tube, we achieve good alignment to form a coaxial geometry. The innermost fluid is pumped through a tapered cylindrical capillary tube, and the middle fluid is pumped through the outer coaxial region (Fig. 1A), which forms a coaxial flow at the exit of the tapered tube. The outermost fluid is pumped through the outer coaxial region from the opposite direction, and all fluids are forced through the exit orifice formed by the remaining inner tube (Fig. 1A). This geometry results in hydrodynamic focusing (24, 32) of the coaxial flow. The flow passes through the exit orifice and subsequently ruptures to form drops; however, the coaxial flow can maintain its integrity and generate double emulsion droplets within the collection tube. We were also able to produce single emulsions by removing the tapered inner injection tube. In this geometry, our device is reminiscent of the selective withdrawal technique (33). Typical diameters of the exit orifice in our devices range from 20 to 200 μm; however, smaller or larger orifices can also be used, which allows the drop size to be adjusted. For convenience, we used a collection tube whose inner diameter was initially narrow and abruptly widened at a distance equal to one–article diameter downstream. These collection tubes were fabricated by axially heating the end of a cylindrical glass tube; as the glass liquefies, the orifice shrinks. Alternatively, we can use a tapered capillary tube as the collection tube. This can provide additional control, but the alignment of two tapered capillary tubes is more delicate and hence more difficult.

Fig. 1.

Microcapillary geometry for generating double emulsions from coaxial jets. (A) Schematic of the coaxial microcapillary fluidic device. The geometry requires the outer fluid to be immiscible with the middle fluid and the middle fluid to be in turn immiscible with the inner fluid. The geometry of the collection tube (round tube on the left) can be a simple cylindrical tube with a constriction, as shown here, or it can be tapered into a fine point (not shown). The typical inner dimension of the square tube is 1 mm; this matches the outer diameter of the untapered regions of the collection tube and the injection tube. Typical inner diameters of the tapered end of the injection tube range from 10 to 50 μm. Typical diameters of the orifice in the collection tube vary from 50 to 500 μm. (B to E) Double emulsions containing only one internal droplet. The thickness of the coating fluid on each drop can vary from extremely thin (less than 3 μm) as in (B) to significantly thicker. (F and G) Double emulsions containing many internal drops with different size and number distributions. (H) Double emulsion drops, each containing a single internal droplet, flowing in the collection tube. The devices used to generate these double emulsions had different geometries.

We achieved a high degree of control over the resultant double emulsions, varying the diameters of both the outer and inner drops and the number of inner droplets [supporting online material (SOM) text I and fig. S1]. We can produce uniform double emulsions, in which each drop contains a single internal droplet, creating core-shell structures whose drop diameter and shell thickness can be controlled. For example, we can form drops with extremely thin shells; the ratio of shell thickness to outer drop radius can be as low as 3% (Fig. 1B). Alternatively, we can increase the shell thickness up to about 40% of the drop radius (Fig. 1, C to E). We can also vary the number and size of the internal droplets in the double emulsions (Fig. 1, F and G). A stream of double emulsions, each containing a single internal droplet, is shown in Fig. 1H.

To gain insight into the breakup of a coaxial flow, we first considered the formation of single emulsions. We defined two mechanisms of drop formation for our device geometry: dripping and jetting (34, 35). Dripping produces drops close to the entrance of the collection tube, within a single orifice diameter, analogous to a dripping faucet. Droplets produced by dripping are typically highly monodisperse. In contrast, jetting produces a long jet that extends three or more orifice diameters downstream into the collection tube, where it breaks into drops. The jetting regime is typically quite irregular, resulting in polydisperse droplets whose radii are much greater than that of the jet. Jet formation is caused by the viscous stress of the outer fluid, whose viscosity, ηOF, is typically 10 times greater than that of the inner fluids in our experiments. Thus, viscous effects dominate over inertial effects, resulting in a low Reynolds number. The formation of double emulsions is similar to that of single emulsions; however, there are two fluids flowing coaxially, each of which can form drops through either mechanism.

The size distribution of the double emulsions is determined by the breakup mechanism, whereas the number of innermost droplets depends on the relative rates of drop formation of the inner and middle fluids (fig. S1). When the rates are equal, the annulus and core of the coaxial jet break simultaneously, generating a double emulsion with a single internal drop. These types of double emulsions can be generated when both fluids are simultaneously dripping (Fig. 2A) or simultaneously jetting (Fig. 2B) (movies S1 to S4). The dripping and jetting mechanisms are closely related, and the transition between them is induced by varying the flow rate of the outermost fluid QOF. The dripping regime occurs for lower QOF, and increasing QOF focuses the coaxial jet more strongly, thinning the inner stream, which leads initially to smaller double emulsion drops. The radius of the outer emulsion drops, Rdrop, decreases linearly with QOF (Fig. 3, solid circles). However, increasing QOF beyond a threshold value causes the jet to abruptly lengthen, signifying the transition to the jetting regime (36); this results in a discontinuous increase in Rdrop (Fig. 3, solid triangles). In contrast, the radius of the coaxial jet, Rjet, measured near the exit orifice decreases monotonically through the transition (Fig. 3, half-filled symbols). As a result, the frequency of droplet production decreases.

Fig. 2.

Steady-state drop formation mechanisms that result in monodisperse double emulsions with a single internal droplet. (A) Dripping and (B) jetting. In both cases, the rate of drop formation is the same for the inner and middle fluids. The transition between dripping and jetting is controlled by QOF for fixed total flow rates of the inner and middle fluids. The double emulsions in (A) have a polydispersity less than 1% and those in (B) have a polydispersity of about 3%. (Inset at bottom) Pinch-off of the double emulsion drops from the coaxial jet. The same device and same fluids were used for the experiments described in Figs. 2 and 3. The outer fluid used was silicon oil with ηOF = 0.48 Pa·s, the middle fluid was a glycerol-water mixture with ηMF = 0.05 Pa·s, and the inner fluid was silicon oil with ηIF = 0.05 Pa·s. The interfacial tension for the aqueous mixture and silicon oil without surfactants is approximately 20 mN/m. The flow rates of the fluids in (A) are QOF = 2500 μl hour–1, QMF = 200 μl hour–1, and QIF = 800 μl hour–1. The flow rates in (B) are QOF = 7000 μl hour–1, QMF = 800 μl hour–1. We applied these flow rates with stepper-motor–controlled syringe pumps (Harvard Apparatus, Holliston, MA).

Fig. 3.

Drop and jet radii versus the flow rates. The drop and jet radii are scaled by the radius of the orifice and we plotted as a function of QOF, scaled by Qsum, where Qsum = QMF + QIF. Solid circles represent the drop diameter in the dripping regime, and open circles represent the inner droplet diameter in the dripping regime. Solid triangles represent the drop diameter in the jetting regime, and open triangles represent the inner droplet diameter in the jetting regime. The solid line represents the results of the model that predicts the drop size in the dripping regime, and the dashed line represents the results of the model that predicts drop size in the jetting regime. Half-filled circles represent the jet radius in the dripping regime, and half-filled triangles represent the jet radius in the jetting regime. The dotted line is the jet radius predicted for a flat velocity profile, and the dash-dotted line is the jet radius predicted for a parabolic velocity profile. The jet radius was consistently measured at the constriction in the collection tube. (Inset) The evolution of a flat velocity profile into a parabolic velocity profile. The gray core represents the coaxial jet and the labels show the drop formation mechanism that is associated with each velocity profile. For all of the experiments, Qsum was fixed at 1000 μl hour–1 and QIF/QMF was fixed at 4.

We can construct a simple physical model for these phenomena. The classic mechanism of drop formation from a cylindrical fluid thread is through the Rayleigh-Plateau instability (37, 38). This instability is driven by interfacial tension and reduces the total surface area of a fluid thread by breaking it into drops. Thus, fluid cylinders are unstable to axisymmetric perturbations with wavelengths larger than several times the radius of the cylinder itself. Although this is strictly valid only for a jet made up of a single fluid, in our experiments we matched the viscosities of the innermost and middle fluids (ηIF = ηMF), ensuring that the velocity profile of the coaxial jet was equivalent to that of a single fluid, and we applied the same considerations to the coaxial fluid cylinder. We also assumed that the fluids are Newtonian. The growth rate of a perturbation is determined by its velocity perpendicular to the interface, v∼ γ/ηOF, where γ is interfacial tension, leading to a droplet pinch-off time of tpinch = CRjetηOF/γ, where C is a constant that depends on the viscosity ratio. Numerical calculations give C≈ 20 when ηIFOF = 0.1 (39). Again, this is strictly valid for a cylinder of a single fluid; for a coaxial fluid thread, the effective interfacial tension may be modified by the fact that there are two interfaces. However, the Rayleigh-Plateau instability cannot occur until the length of the jet has grown to be comparable to its radius. This occurs at growth time Math, where Qsum is the net flow rate of the two inner fluids. If tpinch < tg, droplets will be formed as soon as the jet is large enough to sustain the instability, which will occur right at the outlet; this leads to the dripping regime (Fig. 2A). If tpinch > tg, the jet will grow faster than the droplets can form; this leads to the jetting regime, where the droplets are formed downstream (Fig. 2B). We thus define an effective capillary number of the interface Math(1) where v is the downstream velocity of the inner fluids. This equation governs the transition between dripping and jetting, which occurs when Ca ∼ 1. Expressing the control parameter in terms of a capillary number captures the physical picture that the transition from dripping to jetting occurs when viscous stresses on the interface caused by the fluid flow become so large that the Rayleigh-Plateau instability is suppressed in these tube geometries.

Based on this simple physical picture, we can determine Rjet and Rdrop as a function of QOF by considering the velocity flow profiles in both regimes. However, these velocity profiles evolve as the fluids enter and move downstream through the collection tube, necessitating a different treatment for each mechanism.

When the coaxial jet first enters the exit orifice, the velocity profile of the fluids is approximately flat across the channel (Fig. 3, inset). It remains this way for a distance comparable to the orifice radius times the Reynolds number. Thus, in the dripping regime, where drops form very close to the orifice, mass flux is related to cross-sectional area Math(2) where Rorifice is the radius of the exit orifice. The values of Rjet/Rorifice predicted from Eq. 2, with no adjustable parameters, are in good agreement with the measured values in the dripping regime (Fig. 3, dotted line). Comparison of the measured radii of the drops and the coaxial jet shows that Rdrop = 1.87 Rjet. This empirical relationship is consistent with theoretical calculations (40) of Rdrop for the breakup of an infinitely long cylindrical thread in an ambient fluid for ηIFOF = 0.1. From this we can predict Rdrop, which is in good agreement with the data (Fig. 3, solid line). The small discrepancy near the transition probably results from deviation from a flat velocity profile.

In the jetting regime, where drops are formed well downstream, the fluid flow has evolved into the classic parabolic velocity profile of laminar pipe flow. The viscosity difference between the fluids causes the inner coaxial jet to develop a different velocity profile from that of the outer fluid. The full profiles can be determined by solving the Navier-Stokes equations in the low Reynolds number limit (SOM text II). The jet expands slightly as the collection tube widens, modifying the flow profiles; therefore, we assume a constant radius and determine the dependence of the fluid flow rates on the viscosities and Rjet/Rorifice (eq. S1). We can thus predict the jet radii using no adjustable parameters, and obtain good agreement with values measured before the jet has expanded (Fig. 3, dashed-dotted line).

Drop formation in the jetting regime is generally irregular, leading to more polydisperse size distribution. However, quite stable droplet formation can be achieved, occurring at a fixed location on the jet. We believe that this condition occurs because of the geometry of our collection tube, whose diameter rapidly expands after the narrow orifice. This leads to an expansion of the jet diameter and a concomitant decrease in the velocity. As soon as Ca decreases sufficiently to sustain the Rayleigh-Plateau instability, droplets rupture, fixing the location and resulting in quite monodisperse droplets. In the jetting regime, the frequency of rupture decreases, producing droplets that are quite a bit larger than the size of the jet (Fig. 3). It takes time to fill these larger drops, and we can use mass conservation of the dispersed phases and the characteristic time scale for drop break-off to obtain Math. Solving for drop radius gives, Math(3)

This prediction yields excellent agreement with our results, as shown by the dashed line in Fig. 3. Again, there is some discrepancy between the model and data in the region of the transition, which is not described by Eq. 3. However, the predictive capability of these models provides important guidance in creating double emulsions of a desired size.

The ability to produce precision double emulsions creates many opportunities to fabricate new materials. We can control all three flow rates independently, which allows us to vary the number of internal droplets and the shell thickness. In addition, the inner and outer fluids never come into contact, facilitating great flexibility in devising schemes for encapsulation. One of the major benefits of this technique is the ability to fabricate core-shell structures, and these can easily be made into capsules. As an illustrative example, we fabricated a rigid spherical shell by photopolymerizing a polymer [Norland Optical Adhesive (NOA), Norland Products, Cranbury, NJ] in the middle fluid. We diluted the adhesive by 30% with acetone to decrease its viscosity. After generating the double emulsions, we cured the shells with an ultraviolet (UV) light source for approximately 10 s as the double emulsions traversed the collection tube. Brightfield images of the double emulsions and the resulting solid shells are shown in Fig. 4, A and B, respectively. To confirm that we indeed formed solid shells, we crushed the spheres between two microscope cover slides. A scanning electron micrograph (SEM) image confirmed the cracked polymer shells (Fig. 4C).

Fig. 4.

Core-shell structures fabricated from double emulsions generated in our device. (A) Optical photomicrograph of the water-in-oil-in-water double emulsion pre-cursor to solid spheres. The oil consists of 70% NOA and 30% acetone, with a viscosity of approximately 50 mPa·s. (B) Optical photomicrograph of rigid shells made by cross-linking the NOA by exposure to UV light. (C) SEM of the shells shown in (B) after they have been mechanically crushed. The scale bar in (C) also applies to (A) and (B). (D) Brightfield photomicrograph of the water-in-oil-in-water double emulsion precursor to a polymer vesicle. The oil phase consists of a mixture of toluene and tetrahydrofuran at 70/30 v/v with dissolved diblock copolymer (PBA-PAA) at 2% w/v. The viscosity of this mixture was approximately 1 mPa·s. (E) Phase-contrast image of the diblock copolymer vesicle after evaporation of the organic solvents. (F) Phase-contrast image of the deflated vesicle after osmotic stress was applied through the addition of 0.1 M sucrose to the outer fluid. The scale bar in (F) also applies to (D) and (E).

We can also use our device to make polymer vesicles, or polymerosomes (41). We created double emulsions with a single internal drop and dissolved diblock copolymers in the intermediate fluid. We used a volatile fluid as the intermediate phase and subsequently evaporated it, thereby forming polymerosomes. This method is a modified solvent evaporation technique (15) and is similar to a technique that has been used to produce solid polymer spheres from double emulsions (1416, 1921). Because we can precisely control the double emulsion drop morphology, we can produce highly controllable polymerosomes. To illustrate this, we generated water-in-oil-in-water double emulsions, with a middle fluid composed of 70% toluene and 30% tetrahydrofuran (THF). This middle fluid serves as the carrier for a diblock copolymer, poly(butyl acrylate)-b-poly(acrylic acid) (PBA-PAA) (Fig. 4D) (42). As the solvent evaporates, the amphiphilic polymers self-assemble into layers on both interfaces, forming polymerosomes. The concentrations of the diblocks were not precisely adjusted; thus, the polymerosomes were not strictly unilamellar. However, the polymer bilayers were very thin, making it difficult to resolve them in brightfield microscopy. Thus, a phase-contrast image of a typical polymer vesicle is shown in Fig. 4E. To confirm that these structures are indeed polymerosomes, we deflated them with osmotic stress by adding a sucrose solution (0.1 M) to the continuous fluid. The polymerosome from Fig. 4E deflated in this way is shown in Fig. 4F. This technique has a sizeable advantage: The inner and outer fluids remain totally separate, providing for efficient and robust encapsulation. In addition to polymerosomes, it should also be possible to form liposomes from phospholipids in the same manner. Alternatively, other methods to produce robust encapsulants include surface-induced polymerization of either the inner or outer interface or temperature-induced gelation of the inner or middle fluid.

Our microcapillary fluidic device is truly three dimensional, completely shielding the inner fluid from the outer one. It can generate double emulsions dispersed in either hydrophilic or hydrophobic fluids. Its production of double emulsion droplets is limited by the drop formation frequency, which varies between approximately 100 and 5000 Hz. Increasing the production rate requires the operation of parallel devices; for this, a stamping technique (43) would be highly desirable. However, an operational device would require control of the wetting properties of the inner channels. Alternatively, a hybrid device incorporating capillary tubes into the superstructure may offer an alternate means of making devices to produce double emulsions.

Supporting Online Material

SOM Text

Fig. S1

Movies S1 to S4

References and Notes

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