Raw production

Bromohydrins can be prepared direcdy from polyhydric alcohols using hydrobromic acid and acetic acid catalyst, followed by distillation of water and acetic acid (21). Reaction conditions must be carehiUy controlled to avoid production of simple acetate esters (22). The raw product is usually a mixture of the mono-, di-and tribromohydrins. 

Factors which may affect the cost of coal upgrading are environmental considerations such as toxicity, hazardous waste disposal, and carcinogenic properties (131). These and other environmental problems from process streams, untreated wastewaters, and raw products would figure significantly into the cost of commercialization. 

The first stage assures high carbon conversion and optimum slag removal. The second stage reduces the raw product gas temperature to about 1000°C. This latter step helps to improve cold gas efficiency relative to other slurry fed processes and to lower waste heat recovery costs (15—18). 

Canned and frozen foods Metric tons/metric tons of raw product 0.04-0.06... 

The reason for this is simple. If the reaction chemistry is not "clean" (meaning selective), then the desired species must be separated from the matrix of products that are formed and that is costly. In fact the major cost in most chemical operations is the cost of separating the raw product mixture in a way that provides the desired product at requisite purity. The cost of this step scales with the complexity of the "un-mixing" process and the amount of energy that must be added to make this happen. For example, the heating and cooling costs that go with distillation are high and are to be minimized wherever possible. The complexity of the separation is a function of the number and type of species in the product stream, which is a direct result of what happened within the reactor. Thus the separations are costly and they depend upon the reaction chemistry and how it proceeds in the reactor. All of the complexity is summarized in the kinetics. 

MWCNT was first discovered by arc-discharge method of pure carbon and successive discovery of SWCNT was also based on the same method in which carbon is co-evaporated with metallic element. Optimisation of such metallic catalyst has recently been performed. Although these electric arc methods can produce gram quantity of MWCNT and SWCNT, the raw product requires rather tedious purification process. 

After 30 minutes of postreaction, the product was poured on ice. The granuiar mass which precipitated [N-(adamantyi-1)formamide] was sucked off and washed with water. The raw product (37 grams) was then refluxed for 10 hours with a solution of 60 grams of NaOH in 600 ml of diethyletie glycol. 

The combined ethereal phases were washed with water until the wash waters were neutral, dried over sodium sulfate, filtered and evaporated to dryness to obtain 16.80 grams of raw product which was purified by redissolving the product obtained in acetone under reflux and by recrystallization by heating and cooling. 

A colorless, colloidal precipitate was formed and stirred thoroughly for about 15 minutes, whereupon it was filtered by suction. The raw product thus obtained was washed with water until It contained only about Va% water-soluble salts. After drying for 12 hours In a vacuum apparatus at 60°C and under a pressure of 12 mm Hg, the product had the form of hard pieces. The pieces were comminuted to powder in a ball mill and the powder was passed through a sieve (3,600 meshes per cm ). The small residue on the sieve was again pulverized and passed through the same sieve. The yield was 870 g, or 99% of theoretical, calculated on the assumed formula... 

In the cycloheptane series with butyllithium a 1 1 mixture of trans- and ew-adducts was obtained however phenyllithium gave predominately the //raw-product [(trans/cis) 95 5],6. Related studies have also been reported17,18. 

The raw product thus obtained is freed from solvent and water by vacuum distillation (7). The separation of the paraffin is performed under vacuum at temperatures above 220°C in a thin film evaporator (8) in the presence of overheated steam. The paraffin-containing solvent and the paraffin are recirculated to the process without further purification. 

Bromocriptine 2 (0.65 g, 1 mmol) was dissolved in 100 ml of dry ethanol and 60 ml of tetrafluoroboric acid / diethylether complex (85 %) was added while stirring. After standing overnight at RT the solvent was evaporated and the raw product isolated by extraction in the system dichloromethane 12% ammonia in water and evaporated to the dry residue. This residue was applied to the chromatographic column (I.D. = 2 cm, lenght = 20 cm) packed with silicagel and eluted with dichloromethane / ethylacetate =1 1. The fractions containing 2 were evaporated to the dry residue and crystallized from alcohol. 

The recycling of plastic materials becomes more and more important, but unfortunately it is not possible to make materials from the same quality as that of the virgin material. For PVC, this problem is even more pronounced than for other plastics. A process is studied which is able to destroy the waste PVC, but which can recover the most important component of it - chlorine - as a raw product for VCM manufacture, with a very high yield. Most of the energy contained in the PVC can be recovered as electrical power and steam. 4 refs. 

Lee, Y.N. and Wiley, R.C., Betalaine yield from a continuous solid-liquid extraction system as influenced by raw product, post-harvest and processing variables, J. Food ScL, 46, 421, 1981. 

A feasible hydrogenation process was developed for the production of 4,6-diamino resorcinol from 4,6-bisphenylazo resorcinol. In the final process 0.8% catalyst (SQ-6, 10% Pd/C) was nsed in five snbseqnent reactions, this means that the specific catalyst consumption was less than 1 500 with respect to the substrate. The yield of the raw product (diamino resorcinol.2HC1) was quantitative, but its aniline content was 3-6 %, after purification the yield was 74-76%, the purity >99%. Even the color of the product was white. The aniline conld be recycled with more than 80% yield. The key to the improved results is that the hydrogenation was performed in the absence of HCl. After the reaction, the product was treated with HCl under hydrogen, and this procedure improved catalyst life. 

Distributors and wholesalers may act as middlemen, moving raw products from the farmer to the processor or manufacturer, or moving processed food to retailers. They will have information on how much is needed by the manufacturer and what quality. Brokers may also do the marketing and check that stores properly present your product. 

The use of air alone leads to a relatively low calorific value product gas, of the order of 4-6 MJ/mi (LHV basis), which is not attractive for H2 production in view of the large bulk of N2 to be separated from it compared to a preseparation from the air. Only the application of hydrogen in ammonia production would need N2 as cofeedstock. Therefore, in this context only steam- or oxygen-blown gasification concepts are dealt with. The raw product gas can, thus, be produced by an oxygen-blown or indirectly heated steam-blown processes. 

Most tars in the product gas are destroyed by thermal cracking as they pass through the hot reaction zone, and the raw product then exits the gasifier at high temperature. The particulate levels in the product gas are typically low due to the absence of turbulence in the gasifier, but the gas may contain alkali vapors as it exits the hot reaction zone. 

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