Butane production

Eollowing initial installation in 1971, the Phase 1 expansion turbines have proven extremely reliable. The redesign effort of Phase 2 in 1992 incorporated improved aerodynamics and changed inlet guide vane profiles in the expansion turbines. This redesign yielded an additional. 40 to. 50 Bcf of gas per year without any increase in recompression horsepower. This translates to an increase in propane and butane production of an additional 3,600 to 4,500 bbl of liquid without an increase in electrical power consumption. 

Because some hydrocracking occurs, Powerforming also produces saturated C to Q light hydrocarbons. The methane and ethane formed normally are consumed as refinery fuel. Propane and butane products are frequently marketed as LPG. The relative quantities of each of these products vary considerably with feed quality, operating conditions and octane severity. 

The de-butanizer works in a similar manner. The upstream tower (depropanizer) determines the maximum vapor pressure of the butane product. If the concentration of propane-minus is too large in the inlet stream, the vapor pressure of the butane overheads will be too high. Similarly, the concentration of pentanes-plus in the butane will depend upon the... 

TABLE 7.6. Process characteristics for optimised nonanal production (using liquid-liquid biphasic catalysis with ionic liquids) and butanal production (using SILP catalysis) on a 100.000 tons/year scale... 

Geurink and Klumpp used 2-butanol as the proton source in benzene solvent. They found an exothermic protodelithiation of —221 4 kJmoP for w-butyl lithium and —240 5 kJmol for the isomeric iec-butyl lithium to form the same w-butane product. The difference between the protodelithiation enthalpies is 19 6 kJmoP, the same as the difference between the enthalpies of formation of the two alkyl lithiums. From Table 1, the difference is ca 21 kJmoR, in complete agreement. 

Wet gas yield includes dry gas and all propane and butane products. The best linear regression model to predict wet gas yield for catalyst A has the form ... 

Port Neches, Tex.° Borger, Tex.° Neches Butane Products Co. Phillips Petroleum Co. Butylene Butane 100,000 56,200... 

Acetaldehyde is a useful huilding block for acetic aod, acetic anhydride. and chloral Ills currently produced from ethylene, ethanol, propane, and butane Production from acetylene appear to be outdated... 

Several internal olefins were also tried in the reaction shown in eq 1. When the reaction of both cis-or trans-2-butene were run at 230°C, they gave a low (10%) yield of the. 2,3-bis (dichlorophosphino)butane as evidenced by a single 31p nmr peak at 193.6 ppm and a symmetrical l C-NMR spectra. When the reaction temperature is raised to 250°C, both cis-and trans-2-butene yield a compound which has the same 31p and 13c-NMR spectra as 6, indicating a l,2-bis(dichlorophosphino)butane product. Along with this rather complex isomer product change, there is an increase in the amount of butylphosphonous dichloride formed. 

The combination disproportionation ratio is known for this reaction so that from the rate of butane production it is possible to calculate the total rate of this reaction between ethyl radicals. 

Fig.2. Butenes and butane production as a function of butadiene conversion on Pd(lll) (left side) and on Pt(l 11) (right side) at 300K and in a large excess of hydrogen [28,29],...

Table 7. Cost structure of n-butanal production processes [145].

Nevertheless, in comparison with the cobalt technology even the first generation of LPO processes (the expression LPO being coined by BP [266]) proved successful and was promoted by a number of companies (e.g., Celanese, Union Carbide, BASF, Mitsubishi), mostly in parallel. One of the first plants for butanal production belonged to Celanese [192] (later Hoechst-Celanese), closely followed by Union Carbide/Davy Powergas/Johnson Matthey [193] and other companies. 

Substituents can affect the partitioning among the competing reaction paths. The formation of the bicyclo[1.1.0]butane product is favored by radical-stabilizing substituents. ... 

Oxidation of iso-butanal, by-product of n-butanal production by the hydroformylation of propene, also gives peroxyisobutyric acid. The kinetic diagram with ozone as initiator is classical [66]. Kinetic parameters were determined in a temperature range from 10 to 30°C [67]. 

Alklation reactor effluent Distillation n-Butane Product, ... 

Yields and product quality Typical product qualities are 5% butanes in the butenes product and 5% butenes in the butanes product. Higher quality products can be achieved if required. losses are essentially zero. 

The reviewer of the literature faces considerable difficulties. Quite often, those studying the reactions of propane and -butane do not trouble to measure or report product selectivities, and when they are given it is most usually in graphical form, from which numbers of limited accuracy have to be extracted by tedious interpolation. Sometimes only ethane selectivities are quoted. Measurements made in UHV systems seem to be more scattered than those made in conventional equipment, and almost all values have to be converted into the Kempling-Anderson formalism (equations 13.13 and 13.14) to make them comparable. In the accompanying Tables 13.9 and 13.10, most values of F and Tj, are obtained by method (2) above. Although for n-butane products the values of 5i can easily be derived from S2 and 53,they are quoted in the tables to save the reader unnecessary labour. 

Table 13.10 tries to summarise a mass of experimental results for the dependence of n-butane product selectivities on temperature and hydrogen pressure. 

In the reaction of n-butane, product selectivities were not much changed by the introduction of copper, high values of S2 (1.05-1.20) being found at 453-473 K values of F were 0.5 to 0.6 and of 0.75 to 1.0. In one case, values of S) were reported to exceed those of 5i this, while impossible, was not commented on. The same occurrence with platinum catalysts under some conditions has been ascribed to a preferential incorporation of Ci units into the carbon deposit. 

Evidence which was consistent with the postulate of methylene-insertion reactions in the formation of hexanes from pentane and xylene from toluene (both in the liquid phase) has already been mentioned. The formation of the three labeled hexanes from pentane in strict ratio relative to the number of available hydrogen positions on pentane strongly suggested that hot methylene was involved. The butanes product from propane by recoiling C (MacKs,y el cd., 1961) were also found in a ratio corresponding to what might he expected from the reaction of the species in the gas phase. 

We are separating 1000 kmol/h of a feed containing propane, n-butane, and n-pentane. The feed pressure is 4.0 atm This feed is 22.4 mol% propane, 44.7 mol% n-butane, and the remainder n-pentane. In the overall process we plan to recover 99.6% of the propane in the propane product, 99% of the n-butane in the n-butane product, and 99.7% of the n-pentane in the n-pentane product. In column 1 recover 99.5% of the n-butane in the bottoms product. For purposes of your initial mass balances, assume 1) There is no n-pentane in the propane product stream, and 2) There is no propane in the n-pentane product stream Check these guesses after you have run the simulations. Both columns operate at 4.0 atm Operate each column at 1.15 L/D minimum Use the optimum feed stage for each column. 

The objective function (economic value) representing the economic operating margin for the column is shown in Figure 14.2, which is defined as the difference between the value of products (top butane product and pentane bottom pentane product) and costs of feed and energy. The value function features two discontinuities. The first, which occurs when the composition of the bottom product is about 1 % butane, corresponds to a change in the top product from off-spec to on-spec. The second discontinuity occurs when the bottom product becomes off-spec at 5% butane. 

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