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(347b) Co-Processing of Liquid Phase Pyrolysis Oil and Refinery Intermediates in a Continuous Hydrodeoxygenation Reactor

Authors: 
Treusch, K., Graz University of Technology
Schwaiger, N., Graz University of Technology
Nagl, R., Graz, University of Technology
Hammerschlag, B., Graz, University of Technology
Ausserleitner, J., Graz, University of Technology
Huber, A., Graz, University of Technology
Pucher, P., BDI - BioEnergy International GmbH
Siebenhofer, M., Graz University of Technology

Introduction

Biomass
pyrolysis is a suitable pathway for the production of 2nd generation
biofuels.1 During pyrolysis, one of the major products is pyrolysis
oil. Due to its high water content, high corrosivity and other negative
properties, pyrolysis oil needs intensive upgrading prior usage as fuel for
combustion engines.2 To achieve those standards, an upgrading step
is necessary. One way to do so is hydrodeoxygenation (HDO).

BiomassPyrolysisRefinery3

An
overall concept for the production of 2nd generation biofuels based
on liquid phase pyrolysis (LPP) is the BiomassPyrolysisRefinery concept. In the
first step, lignocellulosic biomass is pyrolysed in vacuum gas oil to produce
an unpolar oil, pyrolysis oil and pyrolysis char through the bioCRACK process4.
In the second step, the intermediate products are upgraded5,6. The
bioCRACK process was successfully operated in pilot scale (100 kg/h
lignocellulosic feed) over two years.  HDO of LPP oil has already been
performed continuously in the temperature range of 350°C to 400°C and at liquid
hourly space velocities of 0.5 h-1 to
3 h-1.
To fulfill the requirements of a refinery integration, co-processing of LPP oil
and refinery intermediates has to be investigated.

HDO of
LPP oil and refinery intermediates

To perform co-processing in lab
scale, a paraffin mix and LPP oil were used. HDO was carried out in a plug flow
reactor of Parr Instrument Company on an inline-sulfided metal-oxide catalyst. Operating
parameters were 121.1 bar hydrogen pressure and 400°C. Overall LHSV was 1 h-1,
with 75 wt.% paraffine mix and 25 wt.% LPP oil in the feed.

In Figure 1 the boiling ranges of
the HDO products are compared to the boiling range of the paraffin feed. As the
paraffin feed is already highly hydrogenated, only cracking reactions occurred.
It can be seen, that 25 wt.% LPP oil didn’t have a heavy impact on the product
quality.

Figure 1: Boiling ranges of HDO products compared to
the paraffin feed

1            A. Demirbas, Appl. Energy, 2011, 88,
17–28.

2            Q. Zhang, J. Chang, T. Wang and Y. Xu, Energy
Convers.
Manag., 2007, 48,
87–92.

3            N. Schwaiger, R. Feiner, H.
Pucher and L. Ellmaier, 2015, 1–8.

4            J. Ritzberger, P. Pucher and
N. Schwaiger, 2014, 39, 1189–1194.

5            H. Pucher, N. Schwaiger, R.
Feiner, P. Pucher, L. Ellmaier and M. Siebenhofer, Energy Res., 2014, 31,
3205.

6            R. Feiner, N. Schwaiger, H.
Pucher and L. Ellmaier, 2013, 43, 1–6.

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