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Article

Suzuki–Miyaura Coupling Using Monolithic Pd Reactors and Scaling-Up by Series Connection of the Reactors

by
Aiichiro Nagaki
1,*,
Katsuyuki Hirose
1,
Yuya Moriwaki
1,
Masahiro Takumi
1,
Yusuke Takahashi
1,
Koji Mitamura
2,
Kimihiro Matsukawa
2,
Norio Ishizuka
3 and
Jun-ichi Yoshida
4,*
1
Department of Synthetic Chemistry and Biological Chemistry, Graduate School of Engineering, Kyoto University, Nishikyo-ku, Kyoto 615-8510, Japan
2
Osaka Municipal Technical Research Institute, Electronic Material Research Division, 1-6-50, Morinomiya, Joto-ku, Osaka 536-8553, Japan
3
Emaus Kyoto Inc. R&D, 26 Nishida-cho, Saiin, Ukyo-ku, Kyoto 615-0055, Japan
4
National Institute of Technology, Suzuka College, Shiroko-cho, Suzuka, Mie 510-0294, Japan
*
Authors to whom correspondence should be addressed.
Catalysts 2019, 9(3), 300; https://doi.org/10.3390/catal9030300
Submission received: 2 March 2019 / Revised: 14 March 2019 / Accepted: 19 March 2019 / Published: 25 March 2019
(This article belongs to the Special Issue Catalysts for Suzuki–Miyaura Coupling Reaction)
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Abstract

:
The space integration of the lithiation of aryl halides, the borylation of aryllithiums, and Suzuki–Miyaura coupling using a Pd catalyst supported by a polymer monolith flow reactor without using an intentionally added base was achieved. To scale up the process, a series connection of the monolith Pd reactor was examined. To suppress the increase in the pressure drop caused by the series connection, a monolith reactor having larger pore sizes was developed by varying the temperature of the monolith preparation. The monolithic Pd reactor having larger pore sizes enabled Suzuki–Miyaura coupling at a higher flow rate because of a lower pressure drop and, therefore, an increase in productivity. The present study indicates that series connection of the reactors with a higher flow rate serves as a good method for increasing the productivity without decreasing the yields.

1. Introduction

Recently the chemical synthesis using continuous flow reactors has received significant research interests from both academia and the industry [1,2,3,4,5,6,7,8,9,10,11,12,13,14,15,16,17,18,19,20,21,22,23,24,25,26,27,28,29,30,31,32,33,34,35,36,37,38,39,40,41,42,43,44,45,46,47]. Because of better heat and mass transfer and a shorter residence time, flow processes offer various benefits over conventional batch processes, including increased controllability, safety, and selectivity. A number of synthetic transformations that are difficult or impossible for conventional batch processes have been developed using flow processes [48,49,50,51,52,53,54,55,56,57,58].
Palladium-catalyzed cross-coupling reactions [59,60,61,62,63,64], in particular, using heterogeneous catalysts [65,66,67,68,69], serve as a powerful method for the chemical production of fine chemicals and pharmaceuticals, and several examples of the flow process using supported palladium catalysts [70,71,72,73,74,75,76,77,78,79,80,81,82,83,84,85,86,87] including the Suzuki–Miyaura coupling of arylboronic acids and aryl halides [88,89,90,91] have been reported. Although some arylboronic acids are commercially available, it is often necessary to prepare appropriate arylboronic acids for a desired transformation [92,93,94,95,96,97,98,99], and the preparation of arylbornonic acids often suffers from difficulties in the purification processes [100,101,102,103,104,105]. Therefore, the integration of the preparation of boronic acids and the Suzuki–Miyaura coupling improves the efficiency of the overall transformation. Recently, Buchwald et al. reported the space integration of the preparation of boronic esters by lithiation, borylation, and Suzuki–Miyaura coupling [106]. We have also reported the space integration of the preparation of arylboronic esters bearing electrophilic functional groups based on flash chemistry [107,108,109,110,111,112] using flow microreactors [113]. The overall transformation enables the cross-coupling of two aryl halides bearing electrophilic functional groups. However, homogeneous Pd catalysts are used in both processes. Therefore, it was highly desirable to develop a similar process using heterogeneous Pd catalysts which enable the easy separation and recycling of the catalyst.
Polymer monoliths [114,115,116,117,118,119] serve as ideal supports for reagents and catalysts for continuous flow processes because of their high controllability of surface properties associated with the formation of nano-, micro-, and mesoporous structures. The contact time and temperature can be spatially and temporally controlled throughout the channels. In a preliminary communication, we reported that the space integration [120,121,122] of the preparation of arylboronic esters and Suzuki–Miyaura coupling using a flow reactor packed with the polymer monolith containing an immobilized Pd catalyst [123]. Herein, we report the full details of this study and the process by the series connection of the reactors with high flow rates (Scheme 1).

2. Results and Discussion

2.1. Preparation of Lithium Arylborates Using Flow Microreactors

Prior to studying the Suzuki–Miyaura coupling, we studied the preparation of lithium arylborates by the lithiation of aryl halides followed by the borylation of aryllithiums [113]. The reactions were carried out using a flow microreactor system consisting of two T-shaped micromixers (M1 and M2) and two microtube reactors (R1 and R2) (Figure 1). For example, a solution of bromobenzene (0.10 M in THF, 6.0 mL/min) and a solution of n-BuLi (0.60 M in hexane, 1.0 mL/min) were introduced to M1 (ϕ = 500 μm) at 0 °C by syringe pumps. The resulting solution was passed through R1 (ϕ = 1000 μm, L = 25 cm (tR1 = 1.7 s)) and was mixed with a solution of trimethoxyborane (0.12 M in THF, 5.0 mL/min) in M2 (ϕ = 500 μm). The resulting solution was then passed through R2 (ϕ = 1000 μm, L = 50 cm (tR2 = 2.0 s)). A cloudy mixture was obtained, presumably because of an insufficient solubility of the resulting lithium arylborate (Figure 2a). Various solvents including THF, methanol, and ethanol were examined to solubilize the lithium arylborate, and a clear solution was obtained when methanol was added (Figure 2b).

2.2. Preparation of Polymer Monolith and Immobilization of Pd Catalyst

The preparation of a polymer monolith and the immobilization of a Pd catalyst were carried out as follows (Figure 3). 1,3-Bis(N,N-diglycidylaminomethyl)cyclohexane was added to a solution of poly(ethylene glycol) (PEG, molecular mass = 200), 4,4′-diaminodicyclohexyl-methane, and 6-(phenylamino)-1,3,5-triazine-2,4-dithiol, and the mixture was stirred at room temperature for 30 min. The resultant homogeneous solution was poured into a cylindrical stainless-steel reactor (an empty HPLC column, 4.6 mm ID × 150 mm length). The reactor was annealed to produce epoxy monolithic gels inside. Polymer monolith A was produced by annealing at 100 °C, whereas polymer monolith B was produced by annealing at 85 °C (vide infra). The gelation occurred within 30 min, and the samples were aged at the same temperature for a day. The resulting epoxy monoliths were washed with tetrahydrofuran by using an HPLC pump at 0.1 mL/min for an hour and dried under a vacuum. As shown in Figure 4, the pore size of the gel depends on the annealing temperature. The pore size of monolith B was larger than that of monolith A. Then, monolith A and B were treated with a solution of palladium acetate and were reduced with sodium borohydride. The resulting monolith reactors containing the Pd catalyst were used for Suzuki–Miyaura coupling.

2.3. Suzuki–Miyaura Coupling Using the Pd Catalyst Supported by Polymer Monolith A

Next, we examined the reaction integration of the lithiation of bromobenzene (Ar1–X: Ar1 = C6H5–, X = Br), the arylation of phenyllithiums, and the Suzuki–Miyaura coupling with p-iodobenzonitrile (Figure 5). To the resulting solution of lithium trimethoxy(phenyl)borate was added a solution of p-iodobenzonitrile (Ar2–X: Ar2 = p-NC C6H4–, X = I) (0.033 M in MeOH), and the mixture was passed through the reactor containing the Pd catalyst supported by monolith A at T °C using a plunger pump. The reactions were carried out with various residence times (tR) in the monolith reactor and at various temperatures (T). The residence times were estimated based on the void volume of the reactor.
As profiled in Figure 6, the yield of biphenyl-4-carbonitrile was significantly influenced by both T and tR. At 100 °C, the yield increased with an increase in tR. The coupling product was obtained in good yields (>93%) with tR longer than 4.7 min. The reaction at 120 °C resulted in a slightly better yield (tR = 9.4 min, quantitative yield). Notably, the reaction was complete within a few minutes without using an intentionally added base. Thereafter, the reactions were carried out under two conditions: condition (a) (T = 100 °C, tR = 4.7 min) and condition (b) (T = 120 °C, tR = 9.4 min) for the monolith A catalyst.
The present method was successfully applied to the cross-coupling of various functional aryl and heteroaryl iodides as coupling partners (Table 1). However, the use of phenyl iodide and aryl iodide having an electron-donating group resulted in much lower yields because the coupling reactions for these compounds were much slower. The use of substrates containing an ortho-substituent also showed a similar tendency. The yields for such reactions would be improved with a longer reaction time by connecting the reactors in serial. Notably, a cyano group tolerated the optimized conditions [124], although such functional groups easily undergo decomposition in conventional batch reactions. Therefore, biaryls bearing electrophilic functional groups on both aromatic rings can be synthesized in one flow. In addition, similar present transformations via lithiated heteroaromatics also took place effectively to give the corresponding heterobiaryls in good yields. Furthermore, a triaryl compound having one bromine atom on one of the aromatic rings was also synthesized via the lithiation of 4,4′-dibromobiphenyl, although such a transformation is very difficult when using conventional batch reactors because of the formation of a significant amount of dilithiated species [125].

2.4. Suzuki–Miyaura Coupling Using the Pd Catalyst Supported by Monolith B

The operation of integrated systems consisting of multiple monolithic reactors in series at higher flow rates suffers from a high pressure drop. To solve this problem, a polymer monolith (monolith B) with wider pore sizes was synthesized by changing reaction temperatures when prepared (monolith A for temperature at 100 °C and monolith B for temperature at 85 °C) (vide supra). Generally, the pressure drop depends on the pore size. In fact, the pressure drop of monolith A of a smaller pore size was larger than that of monolith B of a larger pore size. For example, the operation using a monolith A reactor at 60 °C with the flow rate of 1.5 mL/min led to 8.2 Pa, whereas that using a monolith B reactor lead to 0.8 Pa.
Before studying the series connection of the reactors, the reaction using a single monolith B reactor was examined. To a solution of lithium trimethoxy(phenyl)borate prepared by the flow method (Figure 3) was added a solution of p-iodobenzonitrile (0.033 M in MeOH), and the mixture was passed through a reactor containing a Pd catalyst supported by monolith B using a plunger pump (Figure 5). The reactions were carried out with various residence times (tR) at various temperatures (T). As profiled in Figure 7, the yield of biphenyl-4-carbonitrile was significantly influenced by both T and tR. At 100 °C, the yield increased with an increase in tR, and the reaction was complete within a few minutes.

2.5. Series Connection

In general, the productivity can be increased by increasing the flow rate in a single flow reactor (Figure 8a). However, the increase in the flow rate often causes a decrease in the conversion because the residence time in the reactor becomes shorter. Therefore, the numbering-up method with a parallel connection of the flow reactors serves as a common approach to improve the productivity [126,127,128,129,130] (Figure 8b). However, the method often suffers from a poor uniformity in fluid distribution [131,132]. Therefore, various types of flow distributors such as manifold- [133,134], bifurcation-, and split-and-recombine-type flow distributors have been developed to improve the uniformity of the fluid distribution.
We envisaged that the numbering-up method with a series connection of the flow reactors [135] could serve as a method for increasing productivity (Figure 8c). The residence time can be kept constant by a series connection of the reactors even with higher flow rates. A major obstacle of this approach is, however, the increase in the pressure drop with an increase in the number of the reactors in the series. The use of the monolith B reactor solved the problem. Their use in series enabled operation at high flow rates with a low pressure drop.
The reactions were carried out with various flow rates to control the residence time at 100 °C (Figure 9). When a single monolith A reactor was used, the yield of biphenyl-4-carbonitrile was significantly influenced by the flow rate (Table 2, n = 1). The increase in the residence time by decreasing the flow rate caused an increase in the yield. The use of a single monolith B reactor also led to a similar result. Because of the larger pore size, the pressure drop for the monolith B reactor was much lower than that of the monolith A reactor. The product was obtained in a quantitative yield with the flow rate of 0.4 mL/min, although the increase in the flow rate caused a decrease in the yield, presumably because a shorter residence time leads to an incomplete conversion of the substrate.
Next, the reactions were carried out using multiple monolith B reactors connected in series (Table 2, n = 3 and 5). The use of multiple reactors connected in series often caused a higher pressure drop, which might be an obstacle for practical continuous production. However, the pressure drop was acceptable in this case because of larger pore size of monolith B. Notably, by using three reactors connected in series, the product was obtained in a quantitative yield with a flow rate three times larger than that for a single reactor (1.2 mL/min). Therefore, the productivity can be three times higher than that for a single reactor. Similarly, by using five reactors connected in series, the product was obtained in a quantitative yield with a flow rate five times larger than that for a single reactor (2.0 mL/min). Therefore, the productivity was five times larger than that for a single reactor. The increase in the flow rate caused a decrease in the yield because of an incomplete conversion.
The series connection method is also effective in performing reactions which require longer reaction times. For example, the yields of the reactions with iodobenzene and 1-iodo-4-methoxybenzene as an electron-donating coupling partner could be increased by the series connection of three monolith B reactors (Table 3). Other examples are also shown in Table 3.
Moreover, the present method was successfully applied to a gram-scale synthesis of adapalene, which has been used for the treatment of acne, psoriasis, and photoaging (Figure 10). When the coupling of lithium (3-(1-adamantyl)-4-methoxyphenyl)trimethoxyborate and methyl 6-iodo-2-naphthoate was carried out using a single polymer monolith A reactor, a gram scale synthesis was achieved by a 21 h operation (1.55 g, 86% yield). In contrast, by using five monolith B reactors connected in series, a gram scale synthesis was achieved by a 4 h operation (1.49 g, 87% yield). The productivity increased by five times. The hydrolysis of the coupling product with NaOH in 1,2-propanediol gave adapalene in an 89% yield.

2.6. Recyclability of Monolithic Pd Catalysts

The leaching of a catalyst into the reaction stream causing the loss of activity due to the decrease in the catalyst loading is one of the potential problems of flow synthesis using supported catalysts. This is particularly problematic for pharmaceutical production. Thus, there is a great demand for developing robustly supported catalysts. To evaluate the recyclability of the catalyst, the reaction followed by washing with THF was repeated fifteen times, and no significant loss of activity was observed based on the yields of the product as shown in Table 4, indicating that the Pd catalysts supported by the polymer monoliths A and B possess a sufficient stability under the reaction conditions. Therefore, these results mean that Pd leaching would not occur under the present experimental conditions.

3. Materials and Methods

3.1. General

A GC analysis was performed on a SHIMADZU GC-2014 gas chromatograph equipped with a flame ionization detector using a fused silica capillary column (column, CBPI; 0.25 mm × 25 m; initial oven temperature, 50 °C; rate of temperature increase, 10 °C/min; final oven temperature, 250 °C). 1H and 13C NMR spectra were recorded on a Varian MERCURYplus-400 (1H 400 MHz, 13C 100 MHz, Palo Alto, CA, USA) spectrometer with Me4Si or CDCl3 as a standard in CDCl3 unless otherwise noted (see Supplementary Materials). A preparative gel permeation chromatography was performed on a Japan Analytical Industry LC-918 (Tokyo, Japan). THF was purchased from Kanto Chemical Co., Inc. (Tokyo, Japan) as a dry solvent and used without further purification. Hexane was purchased from Wako (Kyoto, Japan), distilled before use, and stored over molecular sieves 4A. Bromobenzene, p-bromobenzonitrile, m-bromobenzonitrile, o-bromobenzonitrile, 4,4′-dibromobiphenyl, 2-bromothiophene, 2-(1-adamantyl)-4-bromoanisole, p-iodobenzonitrile, m-iodobenzonitrile, o-iodobenzonitrile, iodobenzene, methyl 4-iodobenzoate, methyl 2-iodobenzoate, 4-iodoanisole, 2-iodothiophene, 4-iodobenzaldehyde, n-butyllithium phenyllithium, and trimethoxyborane were commercially available. Methyl 6-iodo-2-naphthoate was synthesized according to the literature [136].
Stainless-steel (SUS304) T-shaped micromixers with inner diameters of 250 and 500 μm were manufactured by Sanko Seiki Co., Inc. (Tokyo, Japan). Stainless-steel (SUS316) microtube reactors with inner diameters of 500 and 1000 μm were purchased from GL Sciences (Tokyo, Japan) and were cut into appropriate lengths (3.5, 25, 50, 100, and 300 cm). The micromixers and microtube reactors were connected with stainless steel fittings (GL Sciences, 1/16 OUW) to construct the flow microreactor systems. The flow microreactor system was dipped in the bath to control the temperature. The solutions were continuously introduced to the flow microreactor system using syringe pumps, Harvard PHD 2000, equipped with gastight syringes purchased from SGE or a plunger pump, shimadzu LC-20AT (Tokyo, Japan).

3.2. Preparation of the Pd Catalysts Supported by Monolith A and Monolith B

1,3-Bis(N,N-diglycidylaminomethyl)cyclohexane was added to a solution of poly(ethylene glycol) (PEG, molecular mass = 200) with 4,4′-diaminodicyclohexylmethane and 6-(phenylamino)-1,3,5-triazine-2,4-dithiol, and the mixture was stirred at room temperature for 30 min. The resultant homogeneous solution was poured into a cylindrical stainless-steel reactor (an empty HPLC column, 4.6 mm ID × 150 mm length). The reactor was annealed to the procedure, epoxy monolithic gels inside. Monolith A was produced by annealing at 100 °C, whereas monolith B was produced by annealing at 85 °C. The gelation occurred within 30 min, and the samples were subsequently aged at the same temperature for a day. The epoxy monoliths were washed with THF by an HPLC pump at 0.1 mL/min for an hour and dried under a vacuum. Then, a THF solution of palladium acetate (0.5 wt%, 5 mL) was injected into the monolith reactor at 0.05 mL/min. The monolith reactor adsorbed with palladium acetate was immersed in PEG (molecular mass = 300), heat-treated at 100 °C for 4 h, and was allowed to stand still for overnight at room temperature. THF in the reactor was replaced by PEG300, and the reactor was heat-treated at 200 °C for 4 h and was washed with THF (1 h) and water (1 h) using an HPLC pump at 0.1 mL/min. An aqueous solution of sodium borohydride (0.5 wt%, 5 mL) was injected into the reactor at 0.05 mL/min to reduce palladium ions adsorbed on the surface of the monolith. Then, the reactor was washed with methanol.

3.3. Cross-Coupling of Bromobenzene and p-Iodobenzonitrile by the Space Integation of Lithiation, Borylation, and Suzuki–Miyaura Coupling

A flow microreactor system consisting of two T-shaped micromixers (M1 and M2), two microtube reactors (R1 and R2), and three tube precooling units (P1 (inner diameter ϕ = 1000 μm, length L = 100 cm), P2 (ϕ = 1000 μm, L = 50 cm), and P3 (ϕ = 1000 μm, L = 100 cm)) was used for the formation of lithium borate. A solution of bromobenzene (0.10 M in THF) (flow rate: 6.0 mL/min) and a solution of n-BuLi (0.60 M in hexane) (flow rate: 1.0 mL/min) were introduced to M1 (ϕ = 500 μm) at 0 °C by syringe pumps. The resulting solution was passed through R1 (ϕ = 1000 μm, L = 25 cm (tR1 = 1.7 s)) and was mixed with a solution of trimethoxyborane (0.12 M in THF) (flow rate: 5.0 mL/min) in M2 (ϕ = 500 μm) (0 °C). The resulting solution was passed through R2 (ϕ = 1000 μm, L = 50 cm (tR2 = 2.0 s)) (0 °C). The resulting solution was collected in a vessel. Then, a solution of p-iodobenzonitrile (0.033 M in MeOH (0.67 eq)) was added, and the resulting solution was passed through a flow reactor packed with a Pd catalyst supported by monolith A or monolith B at T °C by using a plunger pump. The reaction was carried out with various residence times (tR) by changing the flow rates at various temperatures (T). After a steady state was reached, the product solution was collected (10 min). The reaction mixture was analyzed by GC, and the results are summarized in Table 5 and Table 6.
Biphenyl-4-Carbonitrile
Synthesized in 52–100% yield (GC yield using an internal standard (tetradecane)); GC tR 21.4 min; 1H NMR (400 MHz, CDCl3) δ 7.76–7.66 (m, 4H), 7.61–7.57 (m, 2H), and 7.52–7.39 (m, 3H). The spectral data were identical to those reported in the literature [137].

3.4. Cross-Coupling of Aryl Bromides (Ar1–Br) and Aryl Halides (Ar2–X) by the Integration of Lithiation, Borylation and Suzuki–Miyaura Coupling in a Flow (Monolith A Reactor)

A flow microreactor system consisting of two T-shaped micromixers (M1 and M2), two microtube reactors (R1 and R2), and three tube precooling units (P1 (inner diameter ϕ = 1000 μm, length L = 100 cm), P2 (ϕ = 1000 μm, L = 50 cm), and P3 (ϕ = 1000 μm, L = 100 cm)) was used for the formation of lithium borate. A solution of arylbromides (Ar1–Br) (0.10 M in THF) (flow rate: 6.0 mL/min) and a solution of n-BuLi (0.60 M in hexane) (flow rate: 1.0 mL/min) were introduced to M1 (ϕ = 250 μm) by syringe pumps. The resulting solution was passed through R1 (1.7 s (ϕ = 1000 μm, L = 25 cm) or 0.059 s (ϕ = 500 μm, L = 3.5 cm)) and was mixed with a solution of trimethoxyborane (0.12 M in THF) (flow rate: 5.0 mL/min) in M2 (ϕ = 250 μm). The resulting solution was passed through R2 (ϕ = 1000 μm, L = 50 cm (tR2 = 2.0 s)) (for the case of 2,2′-dibromobiphenyl, R2 (ϕ = 1000 μm, L = 300 cm (tR2 = 11.8 s)) was used). The resulting solution was collected in a vessel. Then, a solution of arylhalides (Ar2–X) (0.033 M in MeOH (0.67 eq)) was added, and the resulting solution was passed through a flow reactor packed with a polymer monolith A containing immobilized Pd by a plunger pump (condition (a): tR = 4.7 min, T = 100 °C or condition (b): tR = 9.4 min, T = 120 °C). After a steady state was reached, the product solution was collected (10 min) (for the case of 2,2′-dibromobiphenyl, 100 min). The yield of product was determined by GC analysis or isolation. The results are summarized in Table 1.
Methyl 4-Phenylbenzoate
Synthesized in 76% yield (condition (a)) or 87% (condition (b)) (GC yield using an internal standard (tetradecane)); GC tR 22.9 min; 1H NMR (400 MHz, CDCl3) δ 8.13–8.08 (m, 2H), 7.69–7.60 (m, 4H), 7.50–7.36 (m, 3H), and 3.94 (s, 3H). The spectral data were identical to those reported in the literature [138].
Biphenyl
Synthesized in 6% yield (condition (a)) or 41% (condition (b)) (GC yield using an internal standard (tetradecane)); GC tR 17.0 min; 1H NMR (400 MHz, CDCl3) δ 7.62–7.57 (m, 4H), 7.47–7.41 (m, 4H), and 7.38–7.32 (m, 2H). The spectral data were identical to those reported in the literature [139].
4-Methoxybiphenyl
Synthesized in 1% yield (condition (a)) or 29% (condition(b)) (GC yield using an internal standard (tetradecane)); GC tR 20.7 min; 1H NMR (400 MHz, CDCl3) δ 7.58–7.50 (m, 4H), 7.45–7.37 (m, 2H), 7.30 (t, J = 8.0 Hz, 1H), 6.98 (d, J = 8.8 Hz, 2H), and 3.85 (s, 3H). The spectral data were identical to those reported in the literature [140].
2-Phenylthiophene
Synthesized in 86% yield (condition (a)) or 92% (condition (b)) (GC yield using an internal standard (pentadecane)); GC tR 25.6 min; 1H NMR (400 MHz, CDCl3) δ 7.64–7.58 (m, 2H), 7.41–7.35 (m, 2H), 7.33–7.26 (m, 3H), and 7.08 (dd, J = 3.6 Hz, J = 4.8 Hz, 1H). The spectral data were identical to those reported in the literature [141].
4,4′-Dicyanobiphenyl
Synthesized in 68% yield (condition (a)) or 91% (condition (b)) (GC yield using an internal standard (tetradecane)); GC tR 25.4 min; 1H NMR (400 MHz, CDCl3) δ 7.81–7.76 (m, 4H), and 7.72–7.67 (m, 4H). The spectral data were identical to those reported in the literature [142].
3,4′-Dicyanobiphenyl
Synthesized in 17% yield under condition (a) or 83% under condition (b) (GC yield using an internal standard (tetradecane)); GC tR 25.2 min; 1H NMR (400 MHz, CDCl3) δ 7.87 (s, 1H), 7.84–7.75 (m, 3H), 7.72 (d, J = 7.6 Hz, 1H), 7.67 (d, J = 8.0 Hz, 2H), and 7.61 (t, J = 7.6 Hz, 1H); 13C NMR (100 MHz, CDCl3) δ 143.2, 140.4, 132.9, 132.0, 131.5, 130.8, 130.0, 127.8, 118.4, 118.3, 113.5, and 112.2; HRMS (ACPI) calcd. for C14H9N2+ [MH+]: 205.0760, found: 205.0759.
2,4′-Dicyanobiphenyl
Synthesized in 12% yield (condition (a)) or 91% (condition (b)) (GC yield using an internal standard (tetradecane)); GC tR 24.2 min; 1H NMR (400 MHz, CDCl3) δ 7.84–7.78 (m, 3H), 7.74–7.65 (m, 3H), and 7.57–7.50 (m, 2H); 13C NMR (100 MHz, CDCl3) δ 143.3, 142.5, 134.0, 133.2, 132.5, 129.9, 129.6, 128.8, 118.4, 118.0, 112.7, and 111.2; HRMS (ACPI) calcd. for C14H9N2+ [MH+]: 205.0760, found: 205.0758.
Methyl 4-(4-Cyanophenyl)benzoate
Synthesized in 34% yield (condition (a)) or 84% (condition (b)) (GC yield using an internal standard (tetradecane)); GC tR 26.5 min; 1H NMR (400 MHz, CDCl3) δ 8.17–8.12 (m, 2H), 7.78–7.69 (m, 4H), 7.68–7.64 (m, 2H), and 3.96 (s, 3H). The spectral data were identical to those reported in the literature [143].
Methyl 4-(3-Cyanophenyl)benzoate
Synthesized in 15% yield (condition (a)) or 87% (condition (b)) (GC yield using an internal standard (tetradecane)); GC tR 26.3 min; 1H NMR (400 MHz, CDCl3) δ 8.14 (d, J = 8.0 Hz, 2H), 7.90 (s, 1H), 7.84 (d, J = 7.6 Hz, 1H), 7.68 (d, J = 7.6 Hz, 1H), 7.63 (d, J = 8.0 Hz, 2H), 7.58 (t, J = 7.6 Hz, 1H), and 3.95 (s, 3H); 13C NMR (100 MHz, CDCl3) δ 166.6, 143.1, 141.3, 131.6, 131.5, 130.8, 130.4, 130.0, 129.8, 127.1, 118.6, 113.2, and 52.3; HRMS (ACPI) calcd. for C15H11NO2 [M+]: 237.0784, found: 237.0789. The spectral data were identical to those reported in the literature [105].
Methyl 4-(2-Cyanophenyl)benzoate
Synthesized in 2% yield (condition (a)) or 52% (condition (b)) (GC yield using an internal standard (tetradecane)); GC tR 25.6 min; 1H NMR (400 MHz, CDCl3) δ 8.19–8.14 (m, 2H), 7.82–7.78 (m, 1H), 7.71–7.61 (m, 3H), 7.56–7.46 (m, 2H), and 3.96 (s, 3H). The spectral data were identical to those of reported in the literature [144].
1-Cyano-4″-bromo-4,1′:4′,1″-terphenylene
Synthesized in 54% yield (condition (b)) (isolated yield). After the extraction with EtOAc, the crude product was thoroughly washed with hexane and water to give the product as a white solid (59.8 mg); 1H NMR (400 MHz, CDCl3) δ 7.77–7.70 (m, 4H), 7.68 (s, 4H), 7.60 (d, J = 8.8 Hz, 2H), and 7.51 (d, J = 8.8 Hz, 2H). The spectral data were identical to those reported in the literature [145].
2,2′-Bithiophene
Synthesized in 83% yield (condition (a)) or 94% (condition (b)) (GC yield using an internal standard (pentadecane)); GC tR 25.6 min; 1H NMR (400 MHz, CDCl3) δ 7.21 (dd, J = 1.2 Hz, J = 5.2 Hz, 1H), 7.17 (dd, J = 1.2 Hz, J = 3.6 Hz, 1H), and 7.01 (dd, J = 3.6 Hz, J = 5.2 Hz, 1H). The spectral data were identical to those reported in the literature [146].
4-(Thiophen-2-yl)benzonitrile
Synthesized in 78% yield (condition (a)) or 87% (condition (b)) (GC yield using an internal standard (tetradecane)); GC tR 25.6 min; 1H NMR (400 MHz, CDCl3) δ 7.72–7.63 (m, 4H), 7.44–7.38 (m, 2H), and 7.13 (dd, J = 3.6 Hz, J = 5.2 Hz, 1H). The spectral data were identical to those reported in the literature [147].
Methyl 4-(Thiophen-2-yl)benzoate
Synthesized in 71% yield (condition (a)) or 86% (condition (b)) (GC yield using an internal standard (tetradecane)); GC tR 25.6 min; 1H NMR (400 MHz, CDCl3) δ 8.07–8.02 (m, 2H), 7.70–7.65 (m, 1H), 7.42 (dd, J = 1.2 Hz, J = 3.6 Hz, 1H), 7.36 (dd, J = 1.2 Hz, J = 5.2 Hz, 1H), 7.11 (dd, J = 3.6 Hz, J = 5.2 Hz, 1H), and 3.93 (s, 3H); The spectral data were identical to those reported in the literature [148].

3.5. Cross-Coupling of Aryl Bromides (Ar1–Br) and Aryl Halides (Ar2–X) by the Integration of Lithiation, Borylation, and Suzuki–Miyaura Coupling Using a Single Monolith B Reactor or Three Monolith B Reactors Connected in Series

A flow microreactor system consisting of two T-shaped micromixers (M1 and M2), two microtube reactors (R1 and R2), and three tube precooling units (P1 (inner diameter ϕ = 1000 μm, length L = 100 cm), P2 (ϕ = 1000 μm, L = 50 cm), and P3 (ϕ = 1000 μm, L = 100 cm)) was used for the formation of lithium borate. A solution of arylbromides (Ar1Br) (0.10 M in THF) (flow rate: 6.0 mL/min) and a solution of n-BuLi (0.60 M in hexane) (flow rate: 1.0 mL/min) were introduced to M1 (ϕ = 250 μm) by syringe pumps. The resulting solution was passed through R1 (1.7 s (ϕ = 1000 μm, L = 25 cm) or 0.059 s (ϕ = 500 μm, L = 3.5 cm)) and was mixed with a solution of trimethoxyborane (0.12 M in THF) (flow rate: 5.0 mL/min) in M2 (ϕ = 250 μm). The resulting solution was passed through R2 (ϕ = 1000 μm, L = 50 cm (tR2 = 2.0 s)). The resulting solution was collected in a vessel. Then, a solution of arylhalides (Ar2X) (0.033 M in MeOH (0.67 eq)) was added, and the mixing solution was passed through a single monolith B reactor (0.10 mL/min (19.2 min), 120 °C) or three monolith B reactors connected in series (0.10 mL/min (57.6 min), 120 °C). After a steady state was reached, the product solution was collected (10 min). The yield of the product was determined by GC analysis or isolation. The results are summarized in Table 2.
2-Cyano-4′-formylbiphenyl
Synthesized in 65% yield in three monolith B reactors (GC yield using an internal standard (tetradecane)); GC tR 24.0 min; 1H NMR (400 MHz, CDCl3) δ 10.10 (s, 1H), 8.04–8.00 (m, 2H), 7.84–7.80 (m, 1H), 7.76–7.67 (m, 3H), and 7.57–7.50 (m, 2H); 13C NMR (100 MHz, CDCl3) δ 191.7 144.0, 143.9, 136.2, 133.9, 133.0, 130.1, 130.0, 129.5, 128.5, 118.2, and 111.3; HRMS (ACPI) calcd. for C14H10NO+ [MH+]: 208.0762, found: 208.0753. The spectral data were identical to those reported in the literature [149].
2,2′-Dicyanobiphenyl
Synthesized in 63% yield using one reactor or 94% yield using three reactors (GC yield using an internal standard (tetradecane)); GC tR 22.8 min; 1H NMR (400 MHz, CDCl3) δ 7.86–7.81 (m, 2H), 7.73 (td, J = 7.6 Hz, J = 1.2 Hz, 2H), and 7.62–7.56 (m, 4H). The spectral data were identical to those reported in the literature [139].
Methyl 2-(2-Cyanophenyl)benzoate
Synthesized in 43% yield using one reactor or 82% yield using three reactors (GC yield using an internal standard (tetradecane)); GC tR 23.3 min; 1H NMR (400 MHz, CDCl3) δ 8.12–8.07 (m, 1H), 7.74–7.70 (m, 1H), 7.65–7.59 (m, 2H), 7.56–7.50 (m, 1H), 7.46 (td, J = 7.6 Hz, J = 1.2 Hz, 1H), 7.37–7.31 (m, 2H), and 3.71 (s, 3H); 13C NMR (100 MHz, CDCl3) δ 166.9, 145.8, 139.6, 132.3, 132.2, 132.1 131.0, 130.8, 129.6, 129.5, 128.8, 127.5, 118.0, 112.3, and 52.1; HRMS (EI) calcd. for C15H11NO2 [M+]: 237.0790, found: 237.0788.

3.6. Cross-Coupling of Bromobenzene and p-Iodobenzonitrile by the Integration of Lithiation, Borylation, and Suzuki–Miyaura Coupling Using Multiple Monolith B Reactors Connected in Series

A flow microreactor system consisting of two T-shaped micromixers (M1 and M2), two microtube reactors (R1 and R2), and three tube precooling units (P1 (inner diameter ϕ = 1000 μm, length L = 100 cm), P2 (ϕ = 1000 μm, L = 50 cm), and P3 (ϕ = 1000 μm, L = 100 cm)) was used for the formation of lithium borate. A solution of bromobenzene (0.10 M in THF) (flow rate: 6.0 mL/min) and a solution of n-BuLi (0.60 M in hexane) (flow rate: 1.0 mL/min) were introduced to M1 (ϕ = 500 μm) at 0 °C by syringe pumps. The resulting solution was passed through R1 (ϕ = 1000 μm, L = 25 cm (tR1 = 1.7 s)) and was mixed with a solution of trimethoxyborane (0.12 M in THF) (flow rate: 5.0 mL/min) in M2 (ϕ = 500 μm) (0 °C). The resulting solution was passed through R2 (ϕ = 1000 μm, L = 50 cm (tR2 = 2.0 s)) (0 °C). The resulting solution was collected in a vessel. Then, a solution of p-iodobenzonitrile (0.033 M in MeOH (0.67 eq)) was added, and the mixing solution was passed through a flow reactor packed with three or five monolith B reactors connected in series at 100 °C by a plunger pump. The reaction was carried out for various residence times (tR) in the reactor by changing flow rates. After a steady state was reached, the product solution was collected (10 min). The reaction mixture was analyzed by GC, and the results are summarized in Table 3.

3.7. Synthesis of Adapalene

A flow microreactor system consisting of two T-shaped micromixers (M1 and M2), two microtube reactors (R1 and R2), and three tube precooling units (P1 (inner diameter ϕ = 1000 μm, length L = 100 cm), P2 (ϕ = 1000 μm, L = 50 cm), and P3 (ϕ = 1000 μm, L = 100 cm)) was used for the formation of lithium borate. A solution of 2-(1-Adamantyl)-4-bromoanisole (0.10 M in THF) (flow rate: 6.0 mL/min) and a solution of n-BuLi (0.60 M in hexane) (flow rate: 1.0 mL/min) were introduced to M1 (ϕ = 500 μm) at 0 °C by syringe pumps. The resulting solution was passed through R1 (ϕ = 1000 μm, L = 50 cm (tR1 = 3.4 s)) and was mixed with a solution of trimethoxyborane (0.12 M in THF) (flow rate: 5.0 mL/min) in M2 (ϕ = 500 μm). The resulting solution was passed through R2 (ϕ = 1000 μm, L = 50 cm (tR2 = 2.0 s)). The resulting solution was collected in a vessel.
Then, a solution of methyl 6-iodo-2-naphthoate (0.033 M in THF/MeOH = 1.5:1) was added, and the mixing solution was passed through a monolithic reactor at 120 °C by a plunger pump. The reaction was carried out using a single monolith A reactor (flow rate: 0.2 mL/min) (residence time: 9.4 min) or five monolith B reactors (flow rate: 1.0 mL/min) (residence time: 9.5 min). After a steady state was reached, the product solution was collected in 21 h (a single monolith A reactor) or 4 h (five monolith B reactors). After the evaporation of the solvents, the crude product was thoroughly washed with MeOH (2 × 150 mL) to give methyl 6-(3-(1-adamantyl)-4-methoxyphenyl)-2-naphthoate (1.55 g (one single monolith A reactor), 1.49 g (five monolith B reactors)).
Methyl 6-(3-(1-adamantyl)-4-methoxyphenyl)-2-naphthoate (0.517 g) and 20 mL of 1,2-propanediol were placed in a flask, and the mixture was heated to 190 °C. The resulting transparent solution was supplemented with 0.534 g of sodium hydroxide in two portions and mixed for 20 min. The mixture was acidified until pH 1 with 6 N HCl. The resulting suspension was mixed for 30 min and washed with hot water (2 × 50 mL). After drying for 12 h at 120 °C, the yield was 0.458 g (89%).
Methyl 6-Iodo-2-naphthoate
1H NMR (400 MHz, CDCl3) δ 8.56 (s, 1H), 8.29 (s, 1H), 8.07 (dd, J = 8.6 Hz, J = 2.0 Hz, 1H), 7.79 (dd, J = 8.8 Hz, J = 2.0 Hz 1H), 7.76 (d, J = 8.4 Hz, 1H), 7.67 (d, J = 8.8 Hz, 1H), and 3.98 (s, 3H); 13C NMR (100 MHz, CDCl3) δ 166.9, 136.7, 136.6, 135.3, 131.1, 130.9, 130.6, 127.9, 127.0, 126.2, 94.7, and 52.3; HRMS (ACPI) calcd. for C12H10IO2 [MH+]: 312.9720, found: 312.9711. The spectral data were identical to those reported in the literature [137].
Methyl 6-(3-(1-Adamantyl)-4-methoxyphenyl)-2-naphthoate
1H NMR (400 MHz, CDCl3) δ 8.61 (s, 1H), 8.07 (dd, J = 8.6 Hz, J = 1.6 Hz, 1H), 8.01 (s, 1H), 7.99 (d, J = 8.4 Hz, 1H), 7.92 (d, J = 8.4 Hz, 1H), 7.80 (dd, J = 8.6 Hz, J = 2.0 Hz, 1H), 7.60 (d, J = 2.4 Hz, 1H), 7.55 (dd, J = 8.0 Hz, J = 2.4 Hz, 1H), 7.00 (d, J = 8.4 Hz, 1H), 3.99 (s, 3H), 3.91 (s, 3H), 2.18 (s, 6H), 2.10 (s, 3H), and 1.57 (s, 6H). The spectral data were identical to those of reported in the literature [150].
6-(3-(1-Adamantyl)-4-methoxyphenyl)-2-naphthoic Acid (Adapalene)
1H NMR (400 MHz, DMSO-d6) δ 13.09 (brs, 1H), 8.58 (s, 1H), 8.21 (s, 1H), 8.14 (d, J = 8.8 Hz, 1H), 8.06 (d, J = 9.2 Hz, 1H), 7.97 (dd, J = 8.4 Hz, J = 1.6 Hz, 1H), 7.88 (dd, J = 8.6 Hz, J = 1.6 Hz, 1H), 7.65 (dd, J = 8.4 Hz, J = 2.4 Hz, 1H), 7.57 (d, J = 2.4 Hz, 1H), 7.11 (d, J = 8.8 Hz, 1H), 3.86 (s, 3H), 2.13 (s, 6H), 2.06 (s, 3H), and 1.75 (s, 6H). The spectral data were identical to those reported in the literature [150].

3.8. Recyclability of the Polymer Monolith A and Monolith B Reactors

The mixing solution of phenyllithium (0.050 M in Et2O/THF = 1:19 (1.00 eq)), trimethoxyborane (0.050 M in Et2O/THF = 1:19 (1.00 eq)), and p-cyanoiodobenzene (0.033 M in MeOH (0.67 eq)) was passed through a flow reactor packed with a Pd catalyst supported by monolith A or monolith B by using a plunger pump (120 °C, 0.20 mL/min). After a steady state was reached, the product solution was collected (10 min). Then, the monolithic reactor was washed with THF (30 mL). Fifteen cycles of reactions and washings were carried out in the same way. The yields of the product were determined by a GC analysis. The results were summarized in Table 4.

4. Conclusions

An efficient synthetic method of unsymmetrical biaryls was developed by integrating lithiation, borylation, and Suzuki–Miyaura coupling using a flow reactor packed a Pd catalyst supported by the polymer monolith. In addition, a series connection of the flow reactors was proved to be a method for the numbering-up of the flow reactors for a scale-up. The method was successfully applied to various coupling reactions including the synthesis of adapalene. Because both the series connection approach and the conventional parallel connection approach have practical limits of the number of reactors, both approaches will hopefully work together to affect large-scale productions in a continuous flow mode in the industry.

Supplementary Materials

The following are available online at https://www.mdpi.com/2073-4344/9/3/300/s1, Figure S1: 1H NMR spectrum of biphenyl-4-carbonitrile. Figure S2: 1H NMR spectrum of methyl 4-phenylbenzoate. Figure S3: 1H NMR spectrum of biphenyl. Figure S4: 1H NMR spectrum of 4-methoxybiphenyl. Figure S5: 1H NMR spectrum of 2-phenylthiophene. Figure S6: 1H NMR spectrum of 4,4′-dicyanobiphenyl. Figure S7: 1H NMR spectrum of 3,4′-dicyanobiphenyl. Figure S8: 13C NMR spectrum of 3,4′-dicyanobiphenyl. Figure S9: 1H NMR spectrum of 2,4′-dicyanobiphenyl. Figure S10: 13C NMR spectrum of 2,4′-dicyanobiphenyl. Figure S11: 1H NMR spectrum of methyl 4-(4-cyanophenyl)benzoate. Figure S12: 1H NMR spectrum of methyl 4-(3-cyanophenyl)benzoate. Figure S13: 13C NMR spectrum of methyl 4-(3-cyanophenyl)benzoate. Figure S14: 1H NMR spectrum of methyl 4-(2-cyanophenyl)benzoate. Figure S15: 1H NMR spectrum of 1-cyano-4″-bromo-4,1′:4′,1″-terphenylene. Figure S16: 1H NMR spectrum of 2,2′-bithiophene. Figure S17: 1H NMR spectrum of 4-(thiophen-2-yl)benzonitrile. Figure S18: 1H NMR spectrum of methyl 4-(thiophen-2-yl)benzoate. Figure S19: 1H NMR spectrum of 2-cyano-4′-formylbiphenyl. Figure S20: 1H NMR spectrum of 2,2′-dicyanobiphenyl. Figure S21: 1H NMR spectrum of methyl 2-(2-cyanophenyl)benzoate. Figure S22: 13C NMR spectrum of methyl 2-(2-cyanophenyl)benzoate. Figure S23: 1H NMR spectrum of methyl 6-iodo-2-naphthoate. Figure S24: 13C NMR spectrum of methyl 6-iodo-2-naphthoate. Figure S25: 1H NMR spectrum of methyl 6-(3-(1-adamantyl)-4-methoxyphenyl)-2-naphthoate. Figure S26: 1H NMR spectrum of 6-(3-(1-adamantyl)-4-methoxyphenyl)-2-naphthoic acid (Adapalene). Table S1: List of product retention times in GC Analysis.

Author Contributions

Conceptualization, methodology, supervision, project administration and funding acquisition, A.N. and J.-i.Y.; investigation, K.H., Y.M., M.T., Y.T., K.M. (Koji Mitamura), K.M. (Kimihiro Matsukawa), N.I. and A.N.; writing—original draft preparation, A.N. and J.-i.Y.; writing—review and editing, M.T., Y.T. and A.N.

Funding

This work was partially supported by the Grant-in-Aid for Scientific Research on Innovative Areas 2707 Middle molecular strategy from MEXT (no. 15H05849), Scientific Research (B) (no. 26288049), Scientific Research (S) (no. 26220804), Scientific Research (S) (no. 25220913), Scientific Research (C) (no. 17865428), AMED (no. 18061567), the Japan Science and Technology Agency’s (JST) A-step program (no. 18067420), CREST, and the Ogasawara Foundation for the Promotion of Science & Engineering.

Conflicts of Interest

The authors declare no conflict of interest.

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Catalysts 09 00300 sch001 550
Scheme 1. The space integration of the preparation of arylboronic esters and Suzuki–Miyaura coupling by the series connection of a flow reactor packed with the polymer monolith containing an immobilized Pd catalyst.
Scheme 1. The space integration of the preparation of arylboronic esters and Suzuki–Miyaura coupling by the series connection of a flow reactor packed with the polymer monolith containing an immobilized Pd catalyst.
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Catalysts 09 00300 g001 550
Figure 1. The flow microreactor system for the lithiation of bromobenzene (Ar1X) and for borylation (micromixers: M1 and M2, microtube reactors: R1 and R2).
Figure 1. The flow microreactor system for the lithiation of bromobenzene (Ar1X) and for borylation (micromixers: M1 and M2, microtube reactors: R1 and R2).
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Figure 2. A solution of lithium trimethoxy(phenyl)borate (a) before the addition of methanol and (b) after the addition of methanol.
Figure 2. A solution of lithium trimethoxy(phenyl)borate (a) before the addition of methanol and (b) after the addition of methanol.
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Catalysts 09 00300 g003 550
Figure 3. The immobilization of Pd on the polymer monolith in a flow reactor.
Figure 3. The immobilization of Pd on the polymer monolith in a flow reactor.
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Figure 4. (a) A SEM image of monolith A before treatment with Pd(OAc)2, (b) a SEM image of monolith B before treatment with Pd(OAc)2, (c) a SEM image of monolith A after treatment with Pd(OAc)2 followed by a reduction with NaBH4, (d) a TEM image of the cross section of monolith A, and (e) an appearance of the flow reactor containing the Pd catalyst supported by the monolith (size: 4.6 mm ID × 150 mm length).
Figure 4. (a) A SEM image of monolith A before treatment with Pd(OAc)2, (b) a SEM image of monolith B before treatment with Pd(OAc)2, (c) a SEM image of monolith A after treatment with Pd(OAc)2 followed by a reduction with NaBH4, (d) a TEM image of the cross section of monolith A, and (e) an appearance of the flow reactor containing the Pd catalyst supported by the monolith (size: 4.6 mm ID × 150 mm length).
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Catalysts 09 00300 g005 550
Figure 5. The flow microreactor system for lithiation, borylation, and Suzuki–Miyaura coupling using the Pd catalyst supported by the polymer monolith (micromixers: M1 and M2, microtube reactors: R1 and R2).
Figure 5. The flow microreactor system for lithiation, borylation, and Suzuki–Miyaura coupling using the Pd catalyst supported by the polymer monolith (micromixers: M1 and M2, microtube reactors: R1 and R2).
Catalysts 09 00300 g005
Catalysts 09 00300 g006 550
Figure 6. The temperature (T)–residence time (tR) map for the cross-coupling of bromobenzene and p-bromobenzonitrile using the Pd catalyst supported by monolith A: the contour plots with a scattered overlay of the yields of biphenyl-4-carbonitrile (%), which are indicated by small circles.
Figure 6. The temperature (T)–residence time (tR) map for the cross-coupling of bromobenzene and p-bromobenzonitrile using the Pd catalyst supported by monolith A: the contour plots with a scattered overlay of the yields of biphenyl-4-carbonitrile (%), which are indicated by small circles.
Catalysts 09 00300 g006
Catalysts 09 00300 g007 550
Figure 7. The temperature (T)–residence time (tR) map for the cross-coupling of bromobenzene and p-bromobenzonitrile using the Pd catalyst supported by monolith B: the contour plots with a scattered overlay of the yields of biphenyl-4-carbonitrile (%), which are indicated by small circles.
Figure 7. The temperature (T)–residence time (tR) map for the cross-coupling of bromobenzene and p-bromobenzonitrile using the Pd catalyst supported by monolith B: the contour plots with a scattered overlay of the yields of biphenyl-4-carbonitrile (%), which are indicated by small circles.
Catalysts 09 00300 g007
Catalysts 09 00300 g008 550
Figure 8. The increasing productivity of a continuous flow reaction keeping the residence time constant, (a) a single reactor, (b) the numbering-up by parallel connection of the reactors, and (c) the numbering-up by series connection of the reactors.
Figure 8. The increasing productivity of a continuous flow reaction keeping the residence time constant, (a) a single reactor, (b) the numbering-up by parallel connection of the reactors, and (c) the numbering-up by series connection of the reactors.
Catalysts 09 00300 g008
Catalysts 09 00300 g009 550
Figure 9. The flow microreactor system for Suzuki–Miyaura coupling using a single reactor or multiple reactors connected in series (micromixers: M1 and M2, microtube reactors: R1 and R2).
Figure 9. The flow microreactor system for Suzuki–Miyaura coupling using a single reactor or multiple reactors connected in series (micromixers: M1 and M2, microtube reactors: R1 and R2).
Catalysts 09 00300 g009
Catalysts 09 00300 g010 550
Figure 10. The gram scale synthesis of adapalene.
Figure 10. The gram scale synthesis of adapalene.
Catalysts 09 00300 g010
Table
Table 1. The cross-coupling of Ar1–X and Ar2–X using the polymer monolith A containing an immobilized Pd catalyst.
Table 1. The cross-coupling of Ar1–X and Ar2–X using the polymer monolith A containing an immobilized Pd catalyst.
Ar1-XConditions of
Lithiation and Borylation		Ar2-XProductYield (%) a
tR1
(s)		Temperature
(°C)		Condition
(a) c		Condition
(b) d
Catalysts 09 00300 i0011.70 Catalysts 09 00300 i002 Catalysts 09 00300 i00396100
1.70 Catalysts 09 00300 i004 Catalysts 09 00300 i00503
1.70 Catalysts 09 00300 i006 Catalysts 09 00300 i0077687
1.70 Catalysts 09 00300 i008 Catalysts 09 00300 i009641
1.70 Catalysts 09 00300 i010 Catalysts 09 00300 i011129
1.70 Catalysts 09 00300 i012 Catalysts 09 00300 i0138692
Catalysts 09 00300 i0140.0590 Catalysts 09 00300 i015 Catalysts 09 00300 i0166891
0.0590 Catalysts 09 00300 i017 Catalysts 09 00300 i0181783
0.0590 Catalysts 09 00300 i019 Catalysts 09 00300 i0201291
0.0590 Catalysts 09 00300 i021 Catalysts 09 00300 i0223484
Catalysts 09 00300 i0230.0590 Catalysts 09 00300 i024 Catalysts 09 00300 i0256397
0.0590 Catalysts 09 00300 i026 Catalysts 09 00300 i0271587
Catalysts 09 00300 i0280.05924 Catalysts 09 00300 i029 Catalysts 09 00300 i0306398
0.05924 Catalysts 09 00300 i031 Catalysts 09 00300 i032252
Catalysts 09 00300 i0330.0590 Catalysts 09 00300 i034 Catalysts 09 00300 i035054 b
Catalysts 09 00300 i0361.70 Catalysts 09 00300 i037 Catalysts 09 00300 i0388394
1.70 Catalysts 09 00300 i039 Catalysts 09 00300 i0407887
1.70 Catalysts 09 00300 i041 Catalysts 09 00300 i0427186
a Determined by GC. b Isolated yield. c Condition (a): T = 100 °C, tR1 = 4.7 min. d Condition (b): T = 120 °C, tR1 = 9.4 min.
Table
Table 2. The effect of the flow rate for the cross-coupling of bromobenzene and p-iodobenzonitrile using a single monolith reactor and multiple monolith reactors connected in series.
Table 2. The effect of the flow rate for the cross-coupling of bromobenzene and p-iodobenzonitrile using a single monolith reactor and multiple monolith reactors connected in series.
Reactorn (Number of Reactors)Flow Rate
(mL/min)		Residence Time
(min)		Pressure Drop
(MPa)		Yield (%)Productivity
(mg/h)
A10.29.40.99652
A10.44.71.796100
A11.01.93.981220
A11.51.35.966270
B10.29.60.39853
B10.44.80.4100110
B11.01.90.787230
B11.51.30.967270
B30.69.61.498160
B31.24.83.097310
B33.01.96.886690
B34.51.39.055670
B51.09.63.3100270
B52.04.86.699530
B55.01.914751000
B57.51.319521000
a Determined by GC.
Table
Table 3. The cross-coupling of Ar1–X and Ar2–X using a single monolith B reactor or multiple monolith B reactors connected in series.
Table 3. The cross-coupling of Ar1–X and Ar2–X using a single monolith B reactor or multiple monolith B reactors connected in series.
Ar1-XConditions of
Lithiation and Borylation		Ar2-XProductYield (%) a
tR1
(s)		Temperature
(°C)		n = 1n = 3
Catalysts 09 00300 i0431.70 Catalysts 09 00300 i044 Catalysts 09 00300 i0456287
1.70 Catalysts 09 00300 i046 Catalysts 09 00300 i0474174
Catalysts 09 00300 i0480.05924 Catalysts 09 00300 i049 Catalysts 09 00300 i0502665
0.05924 Catalysts 09 00300 i051 Catalysts 09 00300 i0526394
0.05924 Catalysts 09 00300 i053 Catalysts 09 00300 i0544382
a Determined by GC.
Table
Table 4. The recyclability of the polymer monolith A and monolith B containing an immobilized Pd catalyst.
Table 4. The recyclability of the polymer monolith A and monolith B containing an immobilized Pd catalyst.
Cycle NumberYield (%) a
Monolith AMonolith B
19797
296100
39696
410097
597100
69497
79393
89596
99896
109999
119998
129999
139799
149999
159598
a Determined by GC.
Table
Table 5. The cross-coupling of bromobenzene and p-iodobenzonitrile by the sequence of lithiation, borylation, and Suzuki–Miyaura coupling in a flow (monolith A reactor).
Table 5. The cross-coupling of bromobenzene and p-iodobenzonitrile by the sequence of lithiation, borylation, and Suzuki–Miyaura coupling in a flow (monolith A reactor).
T
(°C)		Flow Rate
(mL/min)		tR
(min)		Yield
(%)
600.29.437
0.44.714
1.01.90
1.51.30
800.29.481
0.44.781
1.01.939
1.51.330
1000.29.496
0.44.796
1.01.981
1.51.366
1200.29.4100
0.44.795
1.01.993
1.51.396
Table
Table 6. The cross-coupling of bromobenzene and p-iodobenzonitrile by the sequence of lithiation, borylation, and Suzuki–Miyaura coupling in a flow (monolith B reactor).
Table 6. The cross-coupling of bromobenzene and p-iodobenzonitrile by the sequence of lithiation, borylation, and Suzuki–Miyaura coupling in a flow (monolith B reactor).
T
(°C)		Flow Rate
(mL/min)		tR
(min)		Yield
(%)
600.29.650
0.44.860
1.01.976
1.51.382
800.29.661
0.44.874
1.01.992
1.51.3100
1000.29.667
0.44.887
1.01.9100
1.51.398
1200.29.689
0.44.892
1.01.999
1.51.399

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MDPI and ACS Style

Nagaki, A.; Hirose, K.; Moriwaki, Y.; Takumi, M.; Takahashi, Y.; Mitamura, K.; Matsukawa, K.; Ishizuka, N.; Yoshida, J.-i. Suzuki–Miyaura Coupling Using Monolithic Pd Reactors and Scaling-Up by Series Connection of the Reactors. Catalysts 2019, 9, 300. https://doi.org/10.3390/catal9030300

AMA Style

Nagaki A, Hirose K, Moriwaki Y, Takumi M, Takahashi Y, Mitamura K, Matsukawa K, Ishizuka N, Yoshida J-i. Suzuki–Miyaura Coupling Using Monolithic Pd Reactors and Scaling-Up by Series Connection of the Reactors. Catalysts. 2019; 9(3):300. https://doi.org/10.3390/catal9030300

Chicago/Turabian Style

Nagaki, Aiichiro, Katsuyuki Hirose, Yuya Moriwaki, Masahiro Takumi, Yusuke Takahashi, Koji Mitamura, Kimihiro Matsukawa, Norio Ishizuka, and Jun-ichi Yoshida. 2019. "Suzuki–Miyaura Coupling Using Monolithic Pd Reactors and Scaling-Up by Series Connection of the Reactors" Catalysts 9, no. 3: 300. https://doi.org/10.3390/catal9030300

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