Palladium Promoted Production of Higher Amines from a Lower Amine Feedstock

Abstract

Abstract

The catalytic (Pd/Al₂O₃ and Pd/C; mean Pd size 2.5–3.0 nm from (S)TEM analysis) synthesis of di-butylamine (DBA) and tri-butylamine (TBA) from mono-butylamine (MBA) and DBA, respectively, in continuous gas phase operation is demonstrated. Exclusive production of DBA (from MBA) has been established over both catalysts where 453 ≤ T ≤ 523 K (∆E_a = 79 kJ mol⁻¹). Greater activity for Pd/C is associated with higher levels of surface acidity (from NH₃ chemisorption/TPD) and spillover hydrogen (from H₂ TPD). Reaction of DBA over both catalysts when configured in series delivered full selectivity to TBA. Our results establish a novel clean alternative route for the continuous production of higher (secondary and tertiary) amines.

Graphical Abstract

Introduction

Higher (secondary and tertiary) amines are commercially important in the production of a range of chemical products [1, 2] used in drug production [3] and as solvents in extraction processes [2]. Standard synthesis involves (i) N-alkylation of primary amines with alkyl halides or alcohols [1, 4, 5], (ii) reduction of imines using reducing agents (e.g. NaCNBH₃) in liquid batch mode [3] or hydrogenation of nitriles over supported Pt [6, 7] and Pd [8]. These methods are non-selective and produce amine mixtures. Moreover, they use toxic agents and require complex extraction of the target product with multiple separation/purification steps. Conversion of an amine feedstock to a higher amine product has been considered to a limited extent in the literature and the reaction mechanism is poorly understood. Taking mono-butylamine (MBA) as a model reactant (Fig. 1), dehydrogenation (step 1) generates a reactive butylidenimine (BI) intermediate, which readily reacts with MBA (step 2) to form N-butylidene-butylamine (BBA) with the elimination of 1 mol NH₃. BBA can be hydrogenated (step 3) to di-butylamine (DBA). Tertiary amine synthesis from secondary amines has only been reported by homogeneous catalysis [RuCl₃·xH₂O and P(C₆H₅)] in one patent [9] and we could not find any published reaction mechanism for di-amine to tri-amine transformation. The limited reports on primary amine condensation have employed homogenous catalysts [3, 10–14] that are difficult to recover and reuse. An efficient amine condensation system utilising reusable heterogeneous catalysts in continuous mode at ambient pressure as proposed in this work represents a significant advancement in terms of cleaner processing.

Fig. 1.

Schematic showing the reaction pathways associated with the conversion of mono-butylamine (MBA) to di-butylamine (DBA)

Work to date on the condensation of primary amines over heterogeneous systems suffers from data irreproducibility in terms of temperature control associated with microwave irradiation (of MBA over Pt/C mixed with alumina powder [15]) and the formation of significant amounts of undesired imine by-product (over Cu/Al₂O₃ [16] and Pt/C [10]). Given the established performance of Pd catalysts in dehydrogenation [17–19] and hydrogenation [20–22], critical steps in higher amine synthesis (see Fig. 1), we have adopted Pd/C and Pd/Al₂O₃ as suitable catalyst candidates for this process. Activated carbon [23, 24] and alumina [25–27] supports bear acid sites that favour condensation to generate higher amines [28, 29], as has been shown for acid catalysts (e.g. K-10 montmorillonite [30, 31]). Moreover, electron transfer between the carrier and Pd phase can influence reactant activation and impact on catalytic performance [32] but this effect has not been considered in higher amine production. In this study, we evaluate the feasibility of secondary and tertiary amine production from lower amines in continuous gas phase operation. We compare the catalytic action of Pd/C and Pd/Al₂O₃ and propose a reaction mechanism based on our results. We demonstrate that the use of catalyst beds in series facilitates full selectivity to the higher amine at elevated rates.

Experimental

Catalyst Characterisation

Commercial (1% w/w) Pd/C and Pd/Al₂O₃ catalysts were obtained from Sigma-Aldrich. The Pd content was measured by inductively coupled plasma-optical emission spectrometry (ICP-OES, Vista-PRO, Varian Inc.) from the diluted extract in HF. Catalyst activation by temperature programmed reduction (TPR), H₂ and NH₃ chemisorption, temperature programmed desorption (TPD) and specific surface area (SSA) measurements were carried out in the CHEM-BET 3000 (Quantachrome) unit equipped with a thermal conductivity detector (TCD) for continuous monitoring of gas composition and the TPR Win™ software for data acquisition/manipulation. Samples (0.05–0.1 g) were loaded in a U-shaped Quartz cell (3.76 mm i.d.), outgassed for 30 min and the total SSA recorded in a 30% v/v N₂/He flow with undiluted N₂ (BOC, 99.9%) as internal standard. Two cycles of N₂ adsorption–desorption were employed using the standard single point BET method. TPR was conducted in 17 cm³ min⁻¹ (Brooks mass flow controlled) 5% v/v H₂/N₂ at 2 K min⁻¹ to 573 K [32]. Samples were swept with 65 cm³ min⁻¹ N₂ for 1.5 h, cooled to ambient temperature and subjected to H₂ (BOC, 99.99%) or NH₃ (BOC, 99.98%) pulse (50–1000 µl) titration. The samples were thoroughly flushed in N₂/He (65 cm³ min⁻¹) to remove weakly bound H₂ or NH₃ and subjected to TPD at 10–50 K min⁻¹ (in 65 cm³ min⁻¹ N₂) to 950–1200 K. SSA and H₂/NH₃ uptake/release values were reproducible to within ±5% and the values quoted represent the mean. Palladium particle morphology (size and shape) was determined by transmission (JEOL JEM 2011 TEM unit) and scanning transmission (JEOL 2200FS field emission gun-equipped TEM unit) electron microscopy, employing Gatan DigitalMicrograph 1.82 for data acquisition/manipulation. Samples for analysis were crushed and deposited (dry) on a holey carbon/Cu grid (300 Mesh). Up to 800 individual Pd particles were counted for each catalyst and the surface area-weighted metal diameter (d _(S)TEM) calculated from

$$d_{\text{(S)TEM}}=\frac{{\sum }_{\text{i}}{n}_{\text{i}}{d}_{\text{i}}^3}{{\sum }_{\text{i}}{n}_{\text{i}}{d}_{\text{i}}^2}$$ 1

where n _i is the number of particles of diameter d _i. X-ray photoelectron spectroscopy (XPS) analyses were conducted on an Axis Ultra instrument (Kratos Analytical) under ultra-high vacuum conditions (<10⁻⁸ Torr) using a monochromatic Al Kα X-ray source (1486.6 eV). The source power was maintained at 150 W and the emitted photoelectrons were sampled from a 750 × 350 µm² area at a take-off angle = 90°. The analyser pass energy was 80 eV for survey spectra (0–1000 eV) and 40 eV for high resolution spectra (Pd 3d _5/2 and 3d _3/2). The adventitious carbon 1s peak was calibrated at 284.5 eV and used as an internal standard to compensate for charging effects.

Catalytic Procedure

Reactions (of MBA and DBA, Sigma-Aldrich, ≥99%) were conducted in situ, immediately after catalyst activation, under atmospheric pressure over the temperature range 453–523 K in a fixed bed vertical glass reactor (i.d. = 15 mm). The reactant was delivered at a fixed calibrated flow rate to the reactor via a glass/Teflon air-tight syringe and Teflon line using a microprocessor controlled infusion pump (Model 100 kd Scientific). A layer of borosilicate glass beads served as preheating zone, ensuring the reactants were vaporised and reached reaction temperature before contacting the catalyst bed. Isothermal conditions (±1 K) were maintained by diluting the catalyst bed with ground glass (75 µm); the ground glass was mixed thoroughly with catalyst before insertion in the reactor. Reaction temperature was continuously monitored using a thermocouple inserted in a thermowell within the catalyst bed. A co-current flow of amine and ultra pure (BOC, >99.99%) H₂ was maintained at total GHSV = 1 × 10⁴ h⁻¹ with an inlet amine molar flow (F) of 3.5–6.1 mmol h⁻¹. The H₂ flow rate was monitored using a Humonics (Model 520) digital flowmeter. The molar Pd (n) to F ratio spanned the range 0.3 × 10⁻³ to 2.5 × 10⁻³ h. In blank tests, passage of MBA or DBA in a stream of H₂ through the empty reactor did not result in any detectable conversion. The reactor effluent was frozen in a liquid N₂ trap for subsequent analysis by capillary GC (Perkin-Elmer Auto System XL chromatograph equipped with a programmed split/splitless injector and FID), employing a DB-1 capillary column (i.d. = 0.33 mm, length = 50 m, film thickness = 0.20 μm). The effluent gas from the DBA reaction was bubbled through a water trap to absorb NH₃ at ambient temperature [33]; pH was monitored (pH meter, Hanna Instruments) with time on-stream [34]. Reactant/product molar fractions (x _i) were obtained using detailed calibration plots (not shown). Fractional conversion (X) is given by

$$X(-)=\frac{{\left[\text{reactant}\right]}_{\text{in}}-{\left[\text{reactant}\right]}_{\text{out}}}{{\left[\text{reactant}\right]}_{\text{in}}}$$ 2

with product selectivity (S _i)

$$S_{\text{i}}(\%)=\frac{N_{\text{i}}·x_{\text{i}}}{\sum N_{\text{i}}·x_{\text{i}}}\times 100$$ 3

where [reactant]_in and [reactant]_out represent the concentration of amine entering (in) and leaving (out) the reactor and N _i is the stoichiometric coefficient for each product. Reactant consumption rate (R) was obtained from

$$R({\text{mol}}_{\text{reactant}}{\text{h}}^{-1}{\text{mol}}_{\text{Pd}}^{-1})=\frac{X\times F}{n}$$ 4

Repeated reactions with different samples from the same batch of catalyst delivered raw data reproducibility and mass balances to within ±6%.

Results and Discussion

Production of DBA from MBA

The existing literature suggests that formation of secondary amines from the corresponding mono-amine is a multi-step process (see Fig. 1), involving dehydrogenation (MBA → BI, step 1), condensation with NH₃ release (BI + MBA → BBA, step 2) and hydrogenation (BBA → DBA, step 3) [10]. Reaction over Pd/C and Pd/Al₂O₃ resulted in the sole formation of DBA from MBA. In contrast, Kamiguchi and co-workers [10], using Pd/C to promote the gas phase condensation of MBA over 573–773 K, obtained BBA as principal and DBA as secondary product (S _DBA < 13%). High temperatures favour desorption of BBA [35] and the exclusivity to DBA that we achieve can be tentatively linked to the lower reaction temperature that allows transformation of BBA without desorption. In terms of catalytic activity, Pd/C (208 mol_MBA h⁻¹ mol_Pd ⁻¹) delivered a greater MBA transformation rate than Pd/Al₂O₃ (154 mol_MBA h⁻¹ mol_Pd ⁻¹). There is evidence in the literature that catalytic activity in hydrogenation [36] and dehydrogenation [37], critical for DBA generation (Fig. 1), is influenced by variations in Pd dispersion. The STEM/TEM images provided in Fig. 2, II) for Pd/C (Fig. 2A) and Pd/Al₂O₃ (Fig. 2B) reveal quasi-spherical particles at the nano-scale with a narrow (1–6 nm) size distribution (Fig. 2, III) and an equivalent mean (2.5–3.0 nm, Table 1). The observed differences in reaction rate can not be explained by variations in Pd size. In prior work [38], we demonstrated that condensation reactions in the conversion of butyronitrile to amines is enhanced by support acidity as has been noted for activated carbon [23, 24] and alumina [25–27]. Ambient temperature NH₃ chemisorption coupled with TPD was used to quantify surface acidity. Ammonia release from Pd/C by TPD matched that chemisorbed and exceeded the amount recorded for Pd/Al₂O₃ (Table 1). Increased surface acidity facilitates condensation (Fig. 1, step 2), which can contribute to the observed higher DBA production rate over Pd/C.

Fig. 2.

Representative (I) medium and (II) high magnification TEM/STEM images with (III) associated Pd size distribution for (A) Pd/C and (B) Pd/Al₂O₃

Table 1.

Physico-chemical properties of Pd/C and Pd/Al₂O₃

Catalyst	Pd/C	Pd/Al2O3
d (S)TEM (nm)	2.5	3.0
NH3 chemisorbed (10−5 mol g−1)	94	52
NH3 TPD (10−5 mol g−1)	92	51
H2 chemisorbed (10−2 mol molPd −1)	27	22
H2 TPD (10−2 mol molPd −1)	849	102
SSA (m2 g−1)	870	145
Pd 3d 5/2 BE (eV)	335.9	334.9

As DBA formation involves hydrogenation of BBA (Fig. 1, step 3), availability of surface reactive hydrogen is an important parameter. Total surface hydrogen was evaluated by H₂ TPD where in both cases H₂ release far exceeded that measured in the chemisorption step (Table 1). This suggests hydrogen spillover, i.e. H₂ dissociation at Pd sites with migration of atomic hydrogen to the support [39]. We can note studies that have established the occurrence of hydrogen spillover on activated carbon [40] and Al₂O₃ [41] supported Pd. Hydrogen desorption from Pd/C was appreciably greater than Pd/Al₂O₃ and can be linked to the higher SSA of Pd/C (Table 1), which can accommodate more spillover [40]. Reaction exclusivity was retained for the two catalysts over the temperature range 453 ≤ T ≤ 523 K and the associated Arrhenius plots are shown in Fig. 3. The resultant apparent activation energy (79 kJ mol⁻¹) converged for both catalysts and is lower than that (100 kJ mol⁻¹) reported for the conversion of mono-pentylamine to di-pentylamine [42]. The results establish that Pd/Al₂O₃ and Pd/C promote the gas phase continuous conversion of MBA solely to DBA. Pd/C delivered a higher DBA production rate, which can be associated with greater surface acidity (from NH₃ chemisorption/TPD) that favours the condensation step and increased surface reactive hydrogen (from H₂ TPD) that serves to promote BBA hydrogenation to DBA.

Fig. 3.

Arrhenius plots for the conversion of mono-butylamine (MBA) to di-butylamine (DBA) over Pd/C (filled circle) and Pd/Al₂O₃ (open circle)

Production of TBA from DBA

Given full selectivity to DBA from MBA, we explored the feasibility of continuous TBA production from DBA as feed. The conversion of DBA over both Pd catalysts generated a mixture of MBA and TBA, which is in line with a patent that serves as the only documented report of tertiary amine formation from secondary amines [9]. In terms of activity, Pd/C again delivered a significantly higher DBA consumption rate (Table 2). Selectivity was independent of DBA conversion (Fig. 4) where Pd/C generated equivalent amounts of TBA and MBA whereas Pd/Al₂O₃ promoted preferential formation of TBA. Based on the product distributions, we propose the reaction mechanism presented in Fig. 5, which involves dehydrogenation (DBA → BBA, step I) and hydrogen mediated disproportionation (BBA + DBA → MBA + TBA, step II). DBA adsorbs on Pd through the lone pair of electrons on N [43] resulting in bond polarisation (N^δ−–C^δ+), leading to dehydrogenation and the formation of BBA. Baiker [44] has established (by FTIR) formation of N-methylidene-methylamine from di-methylamine dehydrogenation (on Cu). Disproportionation of BBA with DBA generates TBA with the release of MBA. Xu et al. [45] working with CuO-NiO-PtO/γ-Al₂O₃ in gas phase operation under conditions similar to those used in this work (i.e. 473 K, 1 atm) demonstrated the formation of an aliphatic amine mixture (N-ethyl-n-butylamine, ethylamine, diethylamine, butylamine, dibutylamine and N,N-diethylbutylamine) via disproportionation of ethylamine + butylamine in hydrogen. Formation of TBA as product follows steps I/II in Fig. 5. The MBA that is generated can undergo combined dehydrogenation/condensation/hydrogenation as shown in Fig. 1 to form DBA. The catalytic results suggest that reaction over Pd/C predominantly follows steps I/II with equi-molar production of TBA and MBA. MBA formed on Pd/Al₂O₃ must undergo reaction (to generate DBA) with an overall greater relative enrichment of TBA in the product stream.

Table 2.

Di-butylamine (DBA) consumption rate (R) and selectivity to tri-butylamine (S _TBA) in single-, double- and triple- Pd/Al₂O₃ and Pd/C bed(s); P = 1 atm, T = 473 K

Catalyst	Pd/C		Pd/Al2O3
	R (molDBA h−1 molPd −1)	S TBA (%)	R (molDBA h−1 molPd −1)	S TBA (%)
Single-bed	489	52	34	70
Double-bed	622	92	43	100
Triple-bed	698	100	–	–

Fig. 4.

Selectivity (S _i, %) to mono-butylamine [MBA (filled square, open square)] and tri-butylamine [TBA (filled triangle, open triangle)] as a function of di-butylamine (DBA) fractional conversion (X) for reaction over Pd/C (solid symbols) and Pd/Al₂O₃ (open symbols); T = 473 K; P = 1 atm

Fig. 5.

Proposed reaction scheme for the transformation of di-butylamine (DBA)

Amine activation is governed by the electronic properties of the metal phase [46] that are, in turn, influenced by interactions with the carrier [32]. XPS analysis was conducted over the Pd 3d binding energy (BE) range in order to establish Pd charge and the resultant profiles are presented in Fig. 6; BE values are given in Table 1. Pd/C (Fig. 6A) exhibited a Pd 3d _5/2 signal (at 335.9 eV) that is 0.7 eV higher than metallic Pd (335.2 eV) [47] indicating electron transfer to the carbon support with the generation of Pd^δ+, as proposed elsewhere for nano-scale (4–12 nm) Pd on carbon [32, 48]. In contrast, Pd/Al₂O₃ (Fig. 6B) is characterised by a Pd 3d _5/2 BE (334.9 eV) that is 0.3 eV lower than the metallic Pd reference, suggesting (partial) support → metal electron transfer. This is in accordance with the reported occurrence of electron-rich Pd^δ− (2–10 nm) on Al₂O₃ [32]. The nitrogen in DBA bearing two electron-donating n-butyl chains is more electron-rich than in MBA [49] with a consequent stronger interaction with Pd^δ+ sites on the carbon support and competition for adsorption sites must result in a displacement of MBA from the surface by DBA. On the other hand, Pd^δ− sites on Al₂O₃ exhibit greater repulsion with respect to DBA relative to MBA where the latter is not displaced from the surface and can be transformed to DBA (Fig. 1). Monitoring the pH of an aqueous trap downstream of the reactor demonstrated greater alkalinity of the exhaust stream for reaction over Pd/Al₂O₃ (pH = 9.5) compared with Pd/C (pH = 7.8), which is consistent with NH₃ production over the former via step 2 in Fig. 1.

Fig. 6.

XPS spectra over the Pd 3d binding energy (BE) region recorded for A Pd/C and B Pd/Al₂O₃

In the proposed reaction scheme, surface reaction of DBA with BBA (step (II) in Fig. 5) results in TBA and MBA production. Operation of a second catalyst bed in series should facilitate conversion of MBA (to DBA) exiting the first bed leading to increased TBA yield. The experimental results obtained are provided in Table 2 where the same total mass of catalyst was divided into N (= 1–3) beds at the same inlet DBA and H₂ flow rate. An increase in overall reaction rate and TBA selectivity was observed with increasing number of beds to attain target tertiary amine exclusivity in a two-bed arrangement for Pd/Al₂O₃ and triple Pd/C bed. This is the first time that full selectivity to a tertiary amine from a secondary amine feedstock has been reported. The higher TBA selectivity achieved over Pd/Al₂O₃ relative to Pd/C (Fig. 4) translated into a requisite lower number of catalyst beds in series to achieve full TBA selectivity.

Conclusions

We have established exclusive formation of higher amines (DBA and TBA) from a lower amine (MBA and DBA, respectively) feedstock over nano-scale Pd (mean size = 2.5–3.0) supported on C and Al₂O₃ in gas phase continuous operation. Full selectivity in the conversion of MBA to DBA was attained over both catalysts with an associated apparent activation energy = 79 kJ mol⁻¹. Reaction over Pd/C delivered a significantly higher DBA production rate, which is explained on the basis of a higher level of surface acidity (from NH₃ chemisorption/TPD) and spillover hydrogen (from H₂ TPD). Exclusive formation of TBA (from DBA) has been achieved over both catalysts where operation of beds in series resulted in higher TBA production rates. A reaction mechanism is proposed that accounts for our experimental observations. The results from this work can serve as a basis for an alternative clean and continuous production of higher amines from a lower amine feedstock.