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Logo of nihpaAbout Author manuscriptsSubmit a manuscriptHHS Public Access; Author Manuscript; Accepted for publication in peer reviewed journal;
 
Chem Commun (Camb). Author manuscript; available in PMC 2010 May 28.
Published in final edited form as:
PMCID: PMC2878177
NIHMSID: NIHMS201206

A dynamic micromixer for arbitrary control of disguised chemical selectivity

Abstract

A new type of dynamic micromixer combining the concepts of parallel multi-lamination and hydrodynamic focusing was developed for arbitrary control of disguised chemical selectivity.

Microreactors are microscopic reaction settings that exhibit unique properties versus traditional macroscopic environments: advantages of microreactors include reduced reagent consumption, high surface-area-to-volume ratios and improved control over mass and heat transfer.18 In addition, fluidic physical phenomena in the microreactors are dramatically different from those observed in the macroscopic reaction apparatuses.911 For instance, the inertial effect in the microfluidic environment is negligible (due to a low value of Reynolds number, Re), and thus fluid transport is dictated by fluid viscosity, leading to laminar flow in microchannels. A microfluidics-based reactor is known to be a turbulence-free system, in which diffusion-driven mixing is relatively slow. As a result, one of the most challenging issues in the field of microreactor design is to facilitate mixing in stand-alone devices. Over the past decades enormous efforts have been devoted to develop micromixers (one type of microreactor) that can be categorized into either active or passive ones.12 Unlike active micromixers, passive ones13 do not require external power, are often composed of robust channel geometry or microstructures, and are developed upon straightforward concepts of increasing contact surfaces and/or shortening the distance for diffusion among different streams. For example, devices based on parallel1416 multi-lamination12 have been developed to achieve efficient mixing.

Mixing may impact reaction outcomes.17,18 A good example is the diazo coupling reaction19 between 4-sulfono-benzenediazonium (1) and 1-naphthol (2) under alkaline conditions at room temperature. This reaction is known as a fast competitive consecutive reaction20 (Scheme 1), where the selectivity between the two major reaction products (i.e., monosubstituted product 3 and disubstituted product 4) is not only determined by intrinsic reaction kinetics21 (k1 = 1.2 × 107 M−1 s−1 and k2 = 2 × 103 M−1 s−1) but also affected by the mixing rates. When reactants 1 and 2 are mixed in a macroscopic setting, the reaction solution is first fragmented by stir-induced turbulence. No matter what mixing approach (e.g., hand mixing or mechanical stirring) is applied, in the best case scenario, the mean radii of the fragmentized solutions are approximately in the range of 100 to 1000 µm,22,23 leading to a mixing time ranging from a millisecond to seconds. Consequently, the fast reaction between the 1 and 2 happens prior to complete homogeneous mixing to give a complicated reaction mixture containing reactant 2 and products 3 and 4. This phenomenon is known as the disguised chemical selectivity. 20,24,25 In order to avoid the undesired disguised chemical selectivity, micromixers exhibiting fast mixing rates have been developed.4,20

Scheme 1
A diazo-coupling reaction between 4-sulfono-1-phenyldiazonium tetrafluorobrate (1) and 1-naphthol (2).

In this paper, we introduce a new concept of a dynamic micromixer (Fig. 1), which combines the concepts of parallel 1416,26 multi-lamination12 and hydrodynamic focusing.18,27 This dynamic mixer composed of 200 µm wide and 80 µm high microchannels was fabricated from poly-methylmethacrylate (PMMA) materials28 or polydimethylsiloxane (PDMS)8 (see ESI). There are three geometrically defined sections in the device, including: (i) a hydrodynamic focusing region where reactant and isolation streams are introduced into the device through the nine inletting microchannels, (ii) a linear microchannel for controlled mixing, and (iii) a triple-branched junction for collecting the resulting reaction mixtures and bypassing the sheath streams. Fluorescence microscopy can be used to observe the flow behavior, and our microreactor, for the first time, can be utilized to control the disguised chemical selectivity a chemical reaction sequence, namely of the diazo coupling reaction between 1 and 2.

Fig. 1
(a) Schematic drawing of our dynamic microreactor composed of three geometrically defined sections: (a) (i) a hydrodynamic focusing region, (ii) a linear microchannel and (iii) a triple-branched junction. (b–f) Fluorescence images of the hydrodynamic ...

To help visualize and characterize the mixing behavior (Fig. 1b–f) within the dynamic microreactor, an aqueous solution containing 5-carboxyfluorescein, was introduced into the reactor from the three reactant inlets along with an isolation solution (i.e., Tris-HCl buffer), and two pairs of sheath streams (pure water) were utilized to compress the three fluorescent and two isolation streams to form a hydrodynamic focused beam (beam width = 9.8 µm) for diffusion-driven mixing. We define the stream compression ratio as α [α = (2QS1 + 2QS2)/(Q1 + 2Qi + 2Q2), in this case α = 20]. Fluorescence microscopy was employed to characterize the flow behavior. As shown in Fig. 1b, three fluorescent streams (representing reagent streams) and two isolation streams formed isolated and parallel laminar flows at the beginning section of the hydrodynamic focusing region.29,30 Sequentially, these laminar flows were compressed into a much smaller characteristic length by two-step hydrodynamic focusing with sheath streams (Fig. 1d and e).31 As a result, the diffusion distances among reactant streams decreased dramatically (Fig. 1f; in principle, each laminar flow can be compressed to as low as 50 nm27). Thus, diffusion-driven mixing results in a homogeneous reaction beam in the linear microchannel. It is important to note that the parabolic effect32 associated with the interactions between reactant streams and microchannel walls has been significantly reduced due to the use of sheath flows which reduce contact areas between reactant streams and microchannel walls.

A systematic study on the relationship between α and the cross-sectional widths of the hydrodynamic focused beam (composed of the three fluorescent reactant and two isolation streams) was conducted (see ESI Fig. S1). Our analyses show that at high α values fast mixing is achieved as suggested by the absence of a visible boundary in between the three fluorescent streams (inset micrographs shown in Fig. S1b). In contrast, three distinct fluorescent streams were observed at low α values, indicating that more time is required to achieve complete mixing for larger diffusion distances. Here, we demonstrate that the mixing timing, mixing speed and entrance length of reagent solutions are determined by the distance between the three reactant streams as a function of the α values. Thus, the sheath streams play a role akin to dynamic channel walls, allowing arbitrary alternation of a virtual microchannel accommodating the five reactant/isolation streams with great precision and stability. These observations constitute the operational principles of our dynamic micromixer, which exhibits unique characteristics, including (i) adjustable mixing time covering from µs to ms, (ii) variable diffusion length, and tunable entrance length for each reactant, (iii) dramatically reduced parabolic effects32 in microchannels, and (iv) dynamically confined reaction spaces at micro/nano scale. It is important to note the use of two-step hydrodynamic focusing confers flow stability to the micromixer compared to the one-step approaches.33 We demonstrated a dynamic operation range covering the stream compression ratio from 1 to 55, corresponding to focused beam widths ranging from 88 to 4 µm. This dynamic mixing property of the microreactor was then utilized to perform fast competitive and consecutive reaction between 1 and 2 under controllable mixing rates. We are able to demonstrate tunable product distributions by methodically altering the mixing rates using the same device configuration.

To allow direct 1H-NMR spectroscopic analyses of the products 3 and 4 obtained from the dynamic micromixer, the reactant/isolation/sheath solutions were prepared in a deuterated solvent mixture (D2O/DMSO-d6 = 8/2, v/v) buffered with Na2CO3 (10 mM) and NaHCO3 (10 mM) to control the reaction condition at a pH value of 10. In our study (Fig. 2a) reactant 1 (30 mM) and 2, (16 mM) were introduced into the respective inlets along with the two isolation streams at an identical flow rate of 1.0 µL min−1, followed by hydrodynamic focusing using two pairs of sheath streams at variable flow rates ranging from 1.5 to 69 µL min−1. By systematically increasing the sheath flows, we studied how different α values (from 1.0 to 55) affect the products distribution of the diazo coupling reaction. The resulting product mixtures were collected from the mixture outlet channel (see ESI Fig. S2b) using NMR tubes, which were kept at −78 °C in the dark prior to 1H-NMR spectroscopic analyses. As references, 1H-NMR spectra of compounds 1, 2, 3 and 4 were recorded in the same buffered deuterated solvent mixture (Fig. S2b). To determine the product distribution ratios (i.e., P3/(2P4 + P3) and P4/(2P4 + P3), where P3 and P4 stand for the molar ratios for the products 3 and 4, respectively) at different α values, we followed the chemical shifts centered at δ = 6.77 and 8.35 ppm, corresponding to the Hj proton of the products 3 and the Hx proton of the product 4, respectively (see ESI, Fig. S2b). The integrations of the 1H-NMR signals gave the product molar ratios, P3 and P4, from which we calculated the product distribution ratios. It is important to note that where conventional methods fail at producing the product of interest, 3, in high yields, our microreactor can produce 3 as the primary product. Fig. 2b and c summarize these experimental results, illustrating the relationship between the stream compression ratio (α) and the resulting product distribution ratios. According to the results obtained in mixing behavior studies (Fig. S2b) and keeping in mind that the α values and hydrodynamic focused beam widths are reciprocally related, the α values can be converted to the respective focused beam widths. Thus Fig. 2c, where the product distribution ratios are plotted against focused beam widths, better interprets the concept of our dynamic micromixer—i.e., multi-lamination beams with variable widths for controllable mixing, allowing arbitrary control of the product distribution of a fast competitive consecutive reaction.4,20

Fig. 2
(a) Competitive-consecutive diazo-coupling reaction between 1 and 2 were carried out in the dynamic reactor at different stream compression ratios (α). (b) Distribution plots of 3 (P3/(2P4 + P3), squares, dashed line) and 4 (P4/(2P4 + P3), triangles, ...

In conclusion, the usefulness of the dynamic microreactor was confirmed by achieving control over the disguised chemical selectivity of the diazo reaction. It is conceivable that this dynamic micromixer can also provide a powerful platform to study particle and quantum dot formation, chemical and biological reaction kinetics and conduct biological analyses, all of which require precise control in reaction kinetics.

Supplementary Material

Experimental

Acknowledgments

This research was supported by the DOD-Defense Threat Reduction Agency (W911NF0610243), the NIH-NCI Nano-Systems Biology Cancer Center (U54A119347). M.S. gratefully acknowledges support by the NSF-PREM Program (Award No. 0351848).

Footnotes

Electronic supplementary information (ESI) available: Experimental. See DOI: 10.1039/b804530e

Notes and references

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