Supporting Information

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1 Supporting Information Highly Active and Selective Zr/MCF Catalyst for Production of 1,3- Butadiene from Ethanol in a Dual Fixed Bed Reactor System Jian Liang Cheong, Yaling Shao, Sherman J. R. Tan, Xiukai Li, Yugen Zhang, and Su Seong Lee* Institute of Bioengineering and Nanotechnology, 31 Biopolis Way, The Nanos, Singapore Table of Contents: Experimental section S2 Figure S S3 Figure S S4 Figure S S5 Table S1 S S6 Figure S S7 Figure S S8 Figure S S9 Figure S7 and S S10 Table S4 and Figure S S11 Figure S S12 S1

2 Experimental section DRIFTS of pyridine absorbed on Zr/MCF: For each spectrum, 80 scans were collected at a resolution of 4 cm -1 from cm -1. About 40 mg of grinded powder (5 wt% of Zr/MCF in KBr) were loaded into the reaction cell. Sample was ramped to 500 C at 20 C/min and soaked for 1 hour, under nitrogen flow of 20 ml/min. Sample was cooled to 100 C and background was taken. Anhydrous pyridine was introduced into the reaction cell at 5 ml N 2 /min until saturation (appearance of the peak at 1578 cm -1 that corresponds to physiosorbed pyridine). After that, the sample was purged with nitrogen to remove physiosorbed pyridine for about 10 mins. A spectrum was then recorded. The reaction cell was heated to various temperatures at 20 C/min and soaked for 10 minutes, before cooling down to 100 C and recording the spectra. Proportion of the strength of the Lewis acid sites was calculated based on the area of the peak at 1606 cm -1, corresponding to Lewis acid (LA) site. Sample calculation: Proportion of Weak LA site = Peak Area 100 C-Peak Area 200 C Peak Area 100 C 100% Proportion of Medium LA site = Peak Area 300 C-Peak Area 200 C Peak Area 100 C 100% Proportion of Strong LA site = Peak Area 300 C Peak Area 100 C 100% S2

3 H b H c H a ppm Figure S1. 1 H NMR spectrum of the products accumulated through bubbling in CDCl 3. S3

4 Figure S2. Control experiment using bare MCF for reactor 1 and Zr/MCF (Zr loading = 2.7 wt%) for reactor 2 at WHSV = 1.5h -1 S4

5 Figure S3. IR spectra of pyridine absorbed on Zr/MCF catalysts with different zirconium loading at four different pyridine desorption temperatures (100, 200, 300 and 400 C). a) Zr/MCF (2.7 wt%) and ZrO 2 at 100 C, b) Zr/MCF (1.4 wt%), c) Zr/MCF (2.7 wt%), d) Zr/MCF (4.3 wt%). S5

6 Table S1. Optimization of the reaction temperature of reactor 1 at a WHSV of 1.5 h -1. Temperature of reactor 2 = 400 C, TOS = 1 h. Temp. Conversion BD AcH Ethene Propene Others EtOH/AcH ( C) (%) (%) (%) (%) (%) (%) Table S2. Optimization of the reaction temperature of reactor 1 at a WHSV of 3.7 h -1. Temperature of reactor 2 = 400 C, TOS = 1 h. Temp. Conversion BD AcH Ethene Propene Others EtOH/AcH ( C) (%) (%) (%) (%) (%) (%) Table S3. Optimization of the reaction temperature of reactor 1 at a WHSV of 1.5 h -1 for 90 v/v% aq. EtOH. Temperature of reactor 2 = 400 C, TOS = 1 h. Temp. Conversion BD AcH Ethene Propene Others EtOH/AcH ( C) (%) (%) (%) (%) (%) (%) S6

7 Figure S4. Conversion and product distribution in the ethanol to butadiene reaction. Reaction conditions: WHSV = 3.7 h -1, temperature of reactor 1 (Cu/MCF) = 250 C, temperature of reactor 2 (Zr/MCF) = 400 C. S7

8 Figure S5. Conversion and product distribution in the ethanol to butadiene reaction by Zr/ Davisil 60 Å. Reaction conditions: WHSV = 3.7 h -1, temperature of reactor 1 (Cu/MCF) = 250 C, temperature of reactor 2 = 400 C. S8

9 Figure S6. Reaction profile when EtOH/H 2 O (90 v/v%) was used as feed. Cu/MCF temperature 240 C. Zr/MCF temperature 400 C. WHSV = 1.5 h -1. S9

10 Figure S7 Nitrogen sorption isotherm of zirconium oxide catalysts on various silica support materials. Figure S8. Thermogravimetric analysis of various Zr/silica catalysts after 15 h run. S10

11 Table S4 Nitrogen sorption data of materials obtained before and after 15 h reaction Support Material BET surface area (m 2 /g) t-plot surface area (m 2 /g) Pore volume a (cm 3 /g) t-plot pore volume (cm 3 /g) MCF MCF (spent) Davisil 60 Å Davisil 60 Å (spent) Davisil 150 Å Davisil 150 Å (spent) Merck silica gel Merck silica gel 60 (spent) a Estimated at the relative pressure of P/P 0 =0.99. Figure S9. Pore size distribution (BJH adsorption branch) of as-prepared and spent Zr/Silica catalysts (after normalization by excluding the weight of coke) S11

12 Figure S10. Conversion and product distribution in the ethanol to butadiene reaction by using 125 mg of Cu/MCF and 375 mg of Zr/MCF. Reaction conditions: WHSV = 1.5 h -1, Temperature of reactor 1 = 240 C, temperature of reactor 2 = 385 C. Flow rate of carrier gas (N 2 ) = 35 ml/min. S12