 As I mentioned before, the evolution of catalytic cracking processes is really a good example of process engineering or reactor design to maximize the thermal efficiency of a process. The first cat cracking process was a batch process introduced in 1915, the McAfee process, where a Lewis acid like aluminum chloride was used in the batch reactor system. But for commercial operation you would need a flow reactor system. So hodry cat cracking was the first commercial continuous process introduced in 1936. The process used the natural alumina silica solids particles as catalysts. And in the process we're going to look at a configuration that has three reactors in parallel. These are fixed bed reactors, essentially filled with the alumina silica pellets, packed with the alumina silica pellets as catalysts. So the gas oil feed is heated in a furnace, in a fired furnace to 800 degrees Fahrenheit. And the feed is fed from the bottom of this packed bed to go through cracking on catalyst surfaces and the products are fed to a fractionator. In the fractionator the products are separated into gas and gasoline and LCO, light cycle oil, as the major products from cat cracking. As the cracking goes on the catalysts are deactivated by coke buildup. And this happens pretty fast within 10 minutes of the introduction of the feed into the reactor. Now since this is an endothermic reaction you would also imagine or you could visualize that the temperature will go down. As the feed moves from the bottom to the top of the reactor. So cracking isn't really very homogeneous because of this decreasing temperature. Now once the catalysts are deactivated within 10 minutes of coke buildup you bring in steam to strip the liquids, somewhat heavy liquids that are sticking onto the catalyst surfaces to remove them into the fractionator and some of this will end up as heavy oil. Once this operation is finished within about 5 minutes then you bring in hot air to burn off the coke to reactivate the catalyst. But to continue the cracking process in the meantime while you are stripping the heavier products and reactivating the catalysts by burning the coke, you need to switch the feed to another reactor. So that is the second in the series. So you have a continuous feed and continuous production through the system using the swing reactor configuration as we refer to. The same thing happens in the second reactor. The catalyst is deactivated within 10 minutes so you bring in the steam to strip the heavier products. And while you are doing that obviously and then later on burning off the coke you should switch the feed to another reactor. That would be the third reactor in the series. And the products are all sent to a fractionator. So by the time the third reactor is coked up you can now switch the feed back to the first reactor. You will have enough time to steam strip and then coke or decoke the first reactor having these additional two reactors in the series. So that is essentially the cycle in the Haudry cat cracking reaction to enable a continuous flow system while the reactors are taken out of service for decoking operations. You see the problem here? The endothermic reaction of cracking is decoupled really from the exothermic reaction of burning off the coke. So for that reason the thermal efficiency of Haudry cat cracking is not very high and it certainly needs to be improved.