Commercial trials

Alakomi, H.L., Skytta, E., Saarela, M., Mattila-Sandholm, T., Latva-Kala, K., and Helander, I.M. 2000. Lactic acid permeabilizes gram-negative bacteria by disrupting the outer membrane. Applied and Environmental Microbiology 66 2001-2005. 

Anonymous. 2005. Preventing foodborne illness. National Provisioner 219 98-102. 

Armstrong, G.L., Hollingsworth, J., and Morris, J.G. 1996. Emerging foodborne pathogens Escherichia coli 0157 H7 as a model of entry of a new pathogen into the food supply of the developed world. Epidemiological Reviews 18 29-51. 

Arroyo, M., Aldred, D., and Magan, N. 2005. Environmental factors and weak organic acid interactions have differential effects on control of growth and ochratoxin A production by Penicillium verrucosum isolates in bread. International ]oumal of Food Microbiology 98 223-231. 

Banerjee, M. and Sarkar, P.K. 2004. Antibiotic resistance and susceptibility to some food preservative measures of spoilage and pathogenic micro-organisms from spices. Food Microbiology 21 335-342. 

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Additive inhibitors have been developed to reduce the contaminant coke produced through nickel-cataly2ed reactions. These inhibitors are injected into the feed stream going to the catalytic cracker. The additive forms a nickel complex that deposits the nickel on the catalyst in a less catalyticaHy active state. The first such additive was an antimony compound developed and first used in 1976 by Phillips Petroleum. The use of the antimony additive reportedly reduced coke yields by 15% in a commercial trial (17). 

The additive approach to reducing SO emissions can be either detrimental or beneficial toward NO reduction. Early alumina-based SO removal additives actually produced substantial increases in NO content in the flue gas (48). The more recent spinel-based SO removal additives have been reported to reduce NO emission by 30% in one commercial trial (49). 

DegOX [Degussa oxidation] A pulp-bleaching process developed by Degussa. The active species is peroxomonosulfuric acid (Caro s acid). The first full-scale commercial trial was held in 1994. 

ECRC, Capenhurst/L B Holliday, Huddersfield pilot and early commercial trials on naphthoquinone and anthraquinone... 

The specifically formulated CGP-1 catalyst plays a vital role in the MIP-CGP process. Unique catalyst design, such as metal promoted MFl zeolite, phosphorus modified Y zeolite, and a novel matrix with excellent capability to accommodate coke [12] were involved to ensure the primary cracking and secondary reactions to proceed within a defined path. The commercial trial results of the MIP-CGP process in SINOPEC Jiujiang Company showed that, in combination with CGP-1 catalyst, the propylene yield was 8.96 wt%, which increased by more than 2.6% as compared with FCC process. The light ends yield and slurry yield are basically equal. The olefin content of the gasoline produced by MIP-CGP process was 15.0 v%, which was 26.1% lower than that of FCC gasoline. The sulfur content of gasoline was decreased from 400 to 270 pg/g. 

Antimony metals passivation technology has been utilized in a variety of FCC unit designs, with a wide range of FCC catalysts (14, 9). In addition, antimony metals passivation has been commercially proven over a broad range of catalyst metals concentrations. As the catalyst metals level increases, the passivation performance improves. A study of over 25 commercial trials revealed that the average hydrogen reduction improved from 35% to 45% as the metals levels increased from less than 6000 ppm (4Ni+V) to over 9000 ppm (4Ni+V), Figure 2. 

Attempts to make adhesive formulations by direct reaction of formaldehyde or its equivalent resulted in products that were excessively viscous, and the working time was too short for commercial application (57). It was concluded that formaldehyde, although readily reactive with the tannin molecule, provided much too short linkages to connect the bulky tannin molecules. This problem was circumvented by the preparation of a polymethylolphenol reagent that, when put in solution with the bark extract, formed a combination that was stable for several weeks at room temperature. When heated, the polymethylolphenol and bark extract reacted rapidly to form an infusible resin. Commercial trials were made to produce exterior-grade Douglas-fir plywood. Widespread use of the extracts for this purpose, however, was inhibited by a drop in the price of phenol below what the bark extracts could be manufactured for. (The best extract for adhesive purposes was an ammonia extract of hemlock bark converted to a sodium derivative prior to spray drying, a more costly extraction procedure than simple sodium hydroxide extraction of bark.)... 

Time Of Flight Secondary Ion Mass Spectrometry (TOF SIMS) analyses of Ecat and RV4+ from a commercial trial. Show that while the vanadium concentration may be higher on the surface of the particles, vanadium is found throughout the RV4+ particle, not only on the outer surface. The SIMS scan also shows that vanadium is found throughout the catalyst particle as well. This shows that over time, there is intraparticle mobility of vanadium in both catalyst and RV4+ particles[5]. 

Seven commercial trials have been conducted using RV4+ technology. A wide range of base catalysts, vanadium levels, unit designs and unit operations, including a partial burn operation, were studied. Table 9 summarizes the key results. 

The wt.% vanadium removed varied from approximately 5-25% and correlated well with the amount of trap in inventory (Figure 6). In all cases, the targeted amount of RV4+in inventory was 5%. While much of our laboratory work was done with 10% blends, a 5% blend was chosen for the commercial trials to minimize possible dilution effects. Several units did not attain the 5% level due to previously scheduled turnarounds. In two of the cases where the targeted level was achieved, Trials A and G, vanadium removal exceeded 20%. Interestingly, the partial burn operation, Trial F, was not that much lower than the full bum operations. 

Based on this successful bench scale program, operation of the demo unit resumed in 2004, following commercial trial manufacture of the newly improved catalyst, demo reactor catalyst replacement, and the completion of required unit modifications to incorporate operational improvements. Several months after its restart, the demo unit continued to run smoothly and continuously under full cyclic operation, with periodic rotational HTR of the reactors. 

CHj=CH—C=N) was commenced by Du Pont in 1940, and by 1942 small quantities of textile fibres were made available for commercial trials. Ethylene, from petroleum cracking, is converted to ethylene oxide which reacts with hydrogen cyanide in the presence of water containing diethylamine and caustic soda at 50°C, to form ethylene cyanhydrin ... 

Previous investigators have drawn attention to the beneficial effect of lime when added in small quantities to asphaltic bitumen. The lime helps retard oxidative hardening (13) and reduces the tendency towards water-stripping (4,11,12). Most asphalts are slightly acidic because of the presence of phenolic or carboxylic substituents and would therefore react with basic oxides to form insoluble salts. For example, Fromm (10) has described the use of iron salts of naphthenic acids as adhesion promoters to improve the water resistance of asphalt concretes. This promising approach is now undergoing commercial trials. The literature also describes methods of chemically modifying asphalt with maleic anhydride or acrylic acid (14), sulfur trioxide (15), sulfur dioxide (16), acetyl sulfate (17-21), and sulfuric acid (20). (For a recent review of the interfacial phenomena in asphaltic compositions see Ref. 4.)... 

The use of calcium as a firming agent for cucumber products began in the 1960 s with commercial trials conducted over several years. 

At the time of writing this paper, three plant trials are currently underway with promising early signs. The sites selected for the trial are spread between Australia and the United States of America in the production of copper in electrowinning and electrorefining plants. Following the completion of these trials in early 2013, it is expected that commercial units will be available for sale by the end of Ql, 2013. All trials to date have been for copper with the next step to include commercial trials in nickel, cobalt and zinc operations. 

Following commercial trials, further development work is underway and will be implemented as required to improve the fimetionality of the HELM tracker system. This includes ... 

Once a new catalyst/product has been identified for evaluation at the manufacturing facility for a commercial trial, the technology teams are expanded to include technical representatives from the polyethylene manufacturing center. These new members will be responsible for implementing the new technology at the commercial scale. For example, a new catalyst needs to be produced in large-scale catalyst preparation facilities in order to produce sufficient catalyst for a commercial trial. This commercial quantity of catalyst is then tested in pilot plant operations to produce polyethylene samples for fabrication into finished products in order to verify that the expected product grades have been produced by the catalyst that will be evaluated in a commercial reactor. 

Note The scale is the amount of polyethylene provided from a developmental program. A pilot plant trial may last 3-7 days and provide sufficient material for fabrication into the end-use product. A commercial trial affords sufficient material for customer evaluation on commercial-scale equipment. 

Commercial trial runs were successfully completed in early 2001 at the PetroChina Daqing Refining Chemical Co. using a revamped DCC unit with a capacity of 80,000 t/a. Three sets of conditions were employed Mode 1 - for maximum propylene yield Mode 3 - for maximum ethylene yield Mode 2 - intermediate between the two. Feedstock properties, major operating parameters and product distribution can be seen in Tables 10, 11 and 12. Across the three modes, the combined yield of ethylene and propylene ranges between 34 and 38 wt% and the total yield of C2 C4" olefins is around 45 wt% in each case. The ethylene to propylene ratio can be adjusted by variation of the operating conditions. 

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