Liquid production capacity

Acetic anhydtide [108-24-7] (CH2C0)20, is a mobile, colorless liquid that has an acrid odor and is a more pierciag lacrimator than acetic acid [64-19-7]. It is the largest commercially produced carboxyUc acid anhydride U.S. production capacity is over 900,000 t yearly. Its chief iadustrial appHcation is for acetylation reactions it is also used ia many other appHcations ia organic synthesis, and it has some utility as a solvent ia chemical analysis. 

A = rate constant (pre-exponential factor from Arrhenius equation k = A exp (-E /RT), sec (i.e., for a first order reaction) B = reduced activation energy, K C = liquid heat capacity of the product (J/kg K)... 

Compared to amorphous silica-alumina catalysts, the zeolite catalysts are more active and more selective. The higher activity and selectivity translate to more profitable liquid product yields and additional cracking capacity. To take full advantage of the zeolite catalyst, refiners have revamped older units to crack more of the heavier, lower-value feedstocks. 

Multistage counter-current liquid-liquid extraction is characterized by a high production capacity and economic efficiency. 

The SDRs reported so far are mainly applicable to liquid reaction systems and their main limitations are short residence times and low production capacities. These problems are addressed by the so-called rotor-stator SDR, which allows a countercurrent gas-liquid contacting at higher throughputs and longer residence times [104]. 

To estimate costs for the liquid-liquid biphasic hydroformylation using ionic liquids, a process was designed for the production of 100,000 tons per year of nonanal. The use of ionic liquids in hydroformylation catalysis is a fairly new technology and exact kinetic data are scarce, thus the TOFs reported for the Rh-sulfoxantphos system [80] have been used to determine catalyst inventory and reactor dimensions. In a similar way the plant design for the SILP process for a production capacity of 100,000 tons per year of butanal has been derived based on preliminary literature results [68]. The process flow sheets for both process variations are shown in Figures 7.12 and 7.13. 

From the steady-state experiments, an equation can be derived for the CIO2 emission (E) involving the following parameters temperature (T), hypochlorite concentration (C), production capacity (P) and liquid level of the reactor (Lv751) ... 

When the capacity is increased under the same process conditions the caustic concentration is increased on higher dosing. As the quantity of free caustic in the end-product and in the liquid flow of the jet-loop reactor is the same, the percentage of caustic reacting with chlorine increases by roughly 25-60% when the production capacity is increased. Depletion of caustic at the liquid-gas interface can then occur more easily. 

The main drawback with the thermochemical route for biomass utilization is the strong dependence on scale-up. To be competitive, the capacity has to be of the order of a small oil refinery (approx. 1 million tonnes per year), but there then exists the problem of the cost of transporting the biomass relatively long distances to this production capacity. Pyrolysis or related technologies ( flash or fast ) could transform biomass into liquid products that are more easily transported, and these liquid products could then be the input for a large, centralized... 

Deep Catalytic Cracking. This process is a variation of fluid catalytic cracking. It uses heavy petroleum fractions, such as heavy vacuum gas oil, to produce propylene- and butylene-rich gaseous products and an aromatic-rich liquid product. The liquid product contains predominandy benzene, toluene, and xylene (see BTX processing). This process is being developed by SINOPEC in China (42,73). SINOPEC is currendy converting one of its fluid catalytic units into a demonstration unit with a capacity of 60,000 t/yr of vacuum gas oil feedstock. 

Production capacity was almost equally split between powdered and nonpowdered activated carbon products. Powdered activated carbon, a less expensive form used in liquid-phase applications, is generally used once and then disposed of. In some cases, however, granular and shaped products are regenerated and reused (35). In 1990 production capacity for granular and shaped products was split with about two-thirds for liquid-phase and one-third for gas-phase applications (37). 

Reference type of ww type of treatment system no, and type of ozone reactors (operating pressure) ozone production capacity nominal// real liquid flow-rate ozone yield coefficient Y(OJM) (M = COD) investment ozonation stage only specific costs (without annuity) remarks... 

During World War II, nine commercial plants were operated in Germany, five using the normal pressure synthesis, two the medium pressure process, and two having converters of both types. The largest plants had capacities of ca 400 m3/d (2500 bbl/d) of liquid products. Cobalt catalysts were used exclusively. 

Worldwide production capacity of liquid polysulfides is about 33,000 t with manufacturing sites in the United States, Japan, and Germany. Total consumption is about 28,600 t. Approximately 50% is for insulating glass sealants, 30% for construction applications, and 10% for aircraft sealants. In addition, 909 t of the solid polysulfide rubbers are sold each year. 

The physical properties normally needed in design and production arc vapor pressure, heal of vaporization, vapor and liquid heal capacity, liquid density, vapor and liquid viscosity. surface tension, and vapt and liquid thermal conductivity. These are plotted graphically against temperature. Ad-... 

Some of the physical properties of fatty acid nitriles are listed in Table 14 (see also Carboxylic acids). Fatty acid nitriles are produced as intermediates for a large variety of amines and amides. Estimated U.S. production capacity (1980) was >140,000 t/yr. Fatty acid nitriles are produced from the corresponding acids by a catalytic reaction with ammonia in the liquid phase. They have little use other than as intermediates but could have some utility as surfactants (qv), mst inhibitors, and plasticizers (qv). 

In the EBMax process, benzene is fed to the bottom of the liquid-filled multibed reactor. Ethylene is co-fed with the benzene and also between the catalyst beds. Polyethylbenzenes, which are almost exclusively diethylbenzenes, undergo transalkylation with benzene in a second reactor. Mobil-Badger offers both liquid phase and vapor phase transalkylation processes. The vapor phase process removes benzene feed coboilers such as cyclohexane and methylcyclopentane as well as propyl and butylbenzenes. Because the EBMax process produces very low levels of propyl and butylbenzenes, for most applications, the more energy efficient liquid phase process is preferred. Worldwide, there are currently ten licensed EBMax units with a cumulative ethylbenzene production capacity of five million metric tons per year. 

The latest industrial application of metathesis was developed by Phillips who started up a plant in late 1985 at Cbannelview, Texas, on the L ondell Petrochemical Complex with a production capacity of 135,000 t/year of propylene from ethylene. This facility carries out the disproportionation of ethylene and 2-butenes, in the vapor phase, around 300 to 350°C, at about 0.5.10 Pa absolute, with a VHSV of 50 to 200 and a once-througb conversion of about 15 per cent 2-butenes are themselves obtained by the dimerization of ethylene in a homogeneous phase, which may be followed by a hydroisomerization step to convert the 1-butene formed (see Sections 13.3.2. A and B). IFP is also developing a liquid phase process in this area. 

Eight Carius tubes (165-mL capacity) were cooled in liquid Nj and evacuated to 0.1 Torr. Phosphane (3 g) and tetrafluoroethene (1 9 g, 90.0 mmol) were condensed into each tube. The tubes w cre scaled and heated at 150 C for 8 h. Following cooling once again to liquid Nj temperature, the tubes were opened, evacuated to 0.1 Torr. and allowed to warm to - 80 C. The gaseous products which distilled were found (IR analysis) to contain octafluorocyclobutane and 1.1.2.2-tetrafluorocthano, in addition to unrcacted phosphane and tetrafluoroethene. The residual liquid products were combined by distillation under reduced pressure into the pot of a 12-inch, spinning-band column. Little or no solid residue remained in the tubes. 

Among the different possibilities for conversion of coal to liquid hydrocarbons, at present only the Fischcr-Tropsch synthesis is performed on a commercial scale. Approximately 2000000 t/a of liquid hydrocarbons are produced at Sasol. Republic of South Africa, and a further increase of production capacity is planned. Due to the present situation in South Africa, which... 

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