Reactor unit

Fig. 6. Catalyst inhibition mechanisms where ( ) are active catalyst sites the catalyst carrier and the catalytic support (a) masking of catalyst (b) poisoning of catalyst (c) thermal aging of catalyst and (d) attrition of ceramic oxide metal substrate monolith system, which causes the loss of active catalytic material resulting in less catalyst in the reactor unit and eventual loss in performance.

Nitrogen Dioxide. Nitrogen dioxide can be formed in the gasifier from the nitrogen present in the coal. Since N02 is an acid gas, it was included in the study as a potential poison. This study was conducted with C150-1-03 in the electric furnace reactor unit. The catalyst was tested under primary wet gas conditions with up to 8 ppm N02 in the dry feed gas. Table XIV provides a synopsis of the test results. 

Fresh feed to recycle gas, ratio of 127 Furnace reactor unit, electric. 58... 

The high pressure continuous reactor consists of five Kenics type in-line static mixers, that were connected in series [3]. Each reactor unit has 27 Kenics elements and dimensions of 19 cm tube length and 3.3 mm inner diameter. Acetonylacetone and 1 % NaOH aqueous solution were pumped into the in-line static mixer reactor using two independent HPLC pumps. The in-line static mixer reactors were immersed in a constant temperature controlled oil bath at 200 °C so that the reaction mixture was heated to the reaction temperature. When the reaction was completed, the fluid was cooled down rapidly in a constant temperature cold bath at 0 °C. At the end of the cooling line, a backpressure regulator was placed to allow experiments to be run at 34 bar. 

The recycle reactor is shown schematically in Figure 1. It consists of a catalytic or electrocatalytic reactor unit with a bypass loop, a recycle pump and a molecular sieve trap unit. The latter comprises one or two packed bed columns in parallel each containing 2-10 g of Linde 5A molecular sieve pellets. On line gas chromatography (Shimadzu 14A) was used for the analysis of CH4, O2, CO, CO2, C2H4 and C2H6 in the reactants and products. 

Vor dem Sprung in die Produktion, Chemie Produktion, December 2002 Prognoses on speed of implementation PAMIRmarket study industry s demands numbering-up risks expert opinions Clariant pigment micro-reactor production smallness not an end in itself general advantages of micro flow industrial process development and optimization share of reactions suited for micro reactors hybrid approach standardized interfaces start of industrial mass production of micro reactors unit construction kit [208],... 

Accordingly, Kumada-Corriu batch processes that need hours can be conducted in micro reactors in a few minutes [2]. 116 mg of product (0.62 mmol) was so produced in only 2 h. Numbering-up to 10 reactor units would give gram quantities. 

Up front capital costs are a critical issue, particularly in our emerging deregulated electricity sector. In Japan, TEPCO reduced the construction time on its newest Advanced Boiling Water Reactor - Unit 7 of the Kashiwazaki Kaariwa Nuclear Power Station - to 51 months. 

Alternatively, a sequence of pervaporation steps can be used to remove the reaction water (Figure 4.10). The reaction solution is pumped through a first fixed-bed reactor and afterwards a pervaporation module is used to remove the water at 80 °C. The solution is subsequently cooled to 60 °C and passed through a second reactor unit. After the next pervaporation step the water content is lowered to 0.2 wt%. By this process, isopropyl myristate is produced from myristyric acid. This and other esters of isopropyl alcohol are used in soaps, skin creams, lubricants and greases [43],... 

In Section 2.2 (this Chapter), we mentioned the difficulties in trying to comply with the new specifications by using single reactor units. From the above discussion, it appears that a second (high-pressure) reactor, with H2S (inter-reactor) scrubbing facilities is the way to go. 

The Syn technology is oriented to the production of ULSD, to the saturation of aromatics and to the improvement of cetane number. These processes can be run in a single reactor unit, in which case, the initial part of the reactor is fed in a co-current way,... 

All the above-mentioned methods will be discussed in this chapter. A number of filtration and reactor units that have been used in published work will be described and an overview of the different membrane materials will be given. As generally catalytic reactions deal with organic substrates and are usually carried out in an organic solvent, the membranes have to be solvent resistant. Thermal stability can also be an issue depending on the process conditions. 

Fig. 12). External numbering-up by flow manifolding to separate reactor units is here one concept for future production reactors with another tenfold increase in structured area.

Calument City, IL, USA, Chemical Plant, Fire Reactor unit fire. 

The fundamental decisions in the synthesis of a multistep process that involves individual reactor units connected in serial and parallel configurations as well as recycle pertain to how the units will be connected. In addition, however, we must consider (for a steady-state process)... 

The contents of the AHSV are continuously recirculated using the agent hydrolysate transfer pump and are returned to the AHSV through a jet mixer. The vessel contents are agitated and maintained at 194°F. The pH is monitored and controlled at all times to eliminate the possibility of agent reformation. Hydrolysate from the AHSV is supplied to the SCWO reactor units in Area 300 through the agent hydrolysate transfer pump. 

Fig. 4 Setup for continuous-flow asymmetric hydrovinylation using an IL/SCCO2 biphasic system. Liquid and gaseous substrates are mixed with the SCCO2 stream before entering the tubular reactor unit and bubbled through the catalyst-containing IL using a capillary. The CO2 flow leaves the reactor on top and the product is collected in a cold trap after controlled expansion to ambient pressure...

When we can predict the response of the reacting system to changes in operating conditions (how rates and equilibrium conversion change with temperature and pressure), when we are able to compare yields for alternative designs (adiabatic versus isothermal operations, single versus multiple reactor units, flow versus batch system), and when we can estimate the economics of these various alternatives, then and only then will we feel sure that we can arrive at the design well fitted for the purpose at hand. Unfortunately, real situations are rarely simple. 

If the size of the production unit requires higher radiant power than can be provided, for technical reasons, by one lamp, clusters of light sources may be installed, which, consequently will alter the diameter or the height of the inner core of, for example, an annular photochemical reactor. However, following the check list of concepts (vide supra), optimal reaction conditions will in most cases limit the size of the photochemical reactor, and the planned rate of production may require several reactor units installed in a parallel mode (batch process) or in series (continuous process). 

Unit output batch reactor Volume stirred-tank reactor Unit output stirred-tank reactor Volume batch reactor... 

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