2. The dwindling supply and exponential growth in the demand of fossil fuels have motivated researchers t o explore alternative resources and technologies for fuels and chemicals. The utilization of the relatively large amounts of glycerol side product (10wt.%) formed in bio-diesel manufacture is a major factor in the overall cost effectiveness of the process. Therefore, use of this glycerol as a renewable feedstock to produce value added chemicals is crucial to biorefinery economics.

3.  Descrition (or glycerin, glycerine) (C3H8O3) : is a simple polyol compound.

4.  Descrition (C 3 H 8 O 2 ): It is a colorless, nearly odorless, clear, viscous liquid with a faintly sweet taste, hygrosc opic and miscible with water, acetone, and chloroform.hygrosc opicmisciblewateracetonechloroform  Ways of obtaining:by catalytic hydrogenolysis  Industry interest: industrial solvent, antifreeze, deicing agent and approved additive in food, cosmetic and ph armaceutical industries

5.  Descrition (CH 2 (CH 2 OH) 2 ): This three-carbon diol is a colorless viscous liquid that is miscible with water.diolmiscible  Ways of obtaining: by bacterial fermentation  Industry interest: Plastics based on this monomer exhi bit better product properties and higher light stability th an those produced by 1,2-propanediol, butanediol or e thylene glycol. 1,3-Propanediol can also be used as a polyglycol-type lubricant and as a solvent.

6. In this assignment, 1,2-PDO has been obtained with two hydrogenlysis methots. We are going to discuss the best aspects of each one

7.  The catalyst in this experiment is an admixture of 5 wt.% Pt/Al2O3 and 5 wt.% Ru/ Al 2 O 3.  The Pt/Al 2 O 3 was chosen to promote the aqueous phase reforming of glycerol to hydrogen, whereas Ru/Al 2 O 3 was chosen to facilitate the hydrogenoly sis of glycerol by in situ hydrogen generated.

8.  It is demonstrate that the admixture catalyst outpe rformed the individual catalysts with respect to 1,2-PDO selectivity and yield under without added hydrogen condition.  The yield of 1,2-PDO was also higher with the admixture catalyst when compared to the externall y added hydrogen condition.

9.  The results with 5% Ru/A l 2 O 3 and 5% Pt/Al 2 O 3 ad mixture combinations an d the monometallic cataly sts on glycerol hydrogen olysis in absence of exter nally added hydrogen at 493 K are compared in these graphs.

10. Glycerol is converted into hydroxyacetone (reaction intermediate) through the dehydration, followed by the hydrogenation into 1,2-propanediol, with a yield over 96%. In this process, the dehydration needs relatively high reaction temperatures, whereas the hydrogenat ion favors low temperatures and high hydrogen concentration.

11.  The main catalyst is Cu/Al 2 O 3, it doesn’t present deactivation until 200ºC and whit that, it would be obtained the best yields and selectivity  The best temperatures for this process are betwee n 170 and 200ºC

12. The production of 1,3 – PDO has been carried out us ing two bacterias: Clostridium butyricum and Klebsie lla pneumoniae

13.  The experiment includes fermentations in batch culture, fed-batch culture and continuous culture.  This experiments were carried out in shake flasks and a fixed-bed bioreactor.  Results showed that the NaCS/PDMDAAC microcapsule has desirable properties such as biomass enrichment in the microcapsule, enhanced substrate tolerance and stable activity of cells respect of the no encapsulated cells.

14.  Maximum concentration of 1,3-propanediol (55–60 g/L) was obtained in batch and fedbatch cultures.  Continuous culture has the advantage of relatively high productivities,however, its 1,3-propanediol concentration is not high enough to reduce the load of downstream separation.  Also, there has been growing interest in a more e conomical route that utilizes glucose as a lower-co st feedstock.

15. The great difference of this bacteria is that it present s a strong tolerance at the inhibitory effect of the 1,3- propanediol and glycerol, even at high concentration s of this substance at the chemostat. It means that 1,3-PDO can be carried out with pure or industrial glycerol. A great advantage for the industry.

16. In this assignment we have studied the production of 1,3- PDO with batch, single-step and two-stage continuous cultures. The medium yield for glycol is 55%, in single-step continuous, large quantities of 1,3-PDO have been obtained with low concentrations of glycerol, however if t he flow increases, the concentration decreases of 1,3 - PDO. having a second stage could be mainly used to further in crease the product concentration and to completely use t he residual glycerol.