Mixed olefin

Propjiene (qv) [115-07-1] is the predominant 0x0 process olefin feedstock. Ethylene (qv) [74-85-1J, as well as a wide variety of terminal, internal, and mixed olefin streams, are also hydroformylated commercially. Branched-chain olefins include octenes, nonenes, and dodecenes from fractionation of oligomers of C —C olefins as well as octenes from dimerization and codimerization of isobutylene and 1- and 2-butenes (see Butylenes). [Pg.465]

Commercially, sulfonic acid ion-exchange resins are used in fixed-bed reactors to make these tertiary alkyl ethers (14). Since the reaction is very selective to tertiary olefins and also reversible, a two-step procedure is also used to recover commercially pure tertiary olefins from mixed olefin process streams. The corresponding tertiary alkyl ether is produced in the olefin mixture and then easily separated from the unreacted olefins by simple fractionation. The reaction is then reversed in a second step to make a commercially pure tertiary olefin, usually isobutylene or isoamylene. [Pg.426]

Dimersol A family of processes for dimerizing single or mixed olefines, catalyzed by mixtures of trialkyl aluminum compounds and nickel salts. Developed by IFP and first commercialized in 1977 by 1997 it was used in 26 plants. [Pg.88]

M. Vichalaik, J.R. Hooper, C.L. Yaws, and R.W. Pike. Alkylation of mixed olefin with isobutane is a STRATCO chemical reactor. In 5th World Congress of Chem. Eng., pages 238-243, San Diego, Cal., July 1996. [Pg.52]

There are three liquid-phase adsorption Sorbex technology-based separation processes for the production of olefins. The first two are the UOP C4 Olex and UOP Sorbutene processes and the third is the detergent Olex process(Cio i,5) [25, 26]. The three olefin separation processes share many similarities. The first similarity between the three olefin separation processes is that each one utilizes a proprietary adsorbent whose empirical formula is represented by Cation,([(A102)),(Si02)2] [27]. The cation type imparts the desired selectivity for the particular separation. This zeolite has a three-dimensional pore structure with pores running perpendicular to each other in the x, y and z planes [28]. The second similarity between the three olefin separation processes is the use of a mixed olefin/paraffin desorbent. The specifics of each desorbent composition are discussed in their corresponding sections. The third similarity is the fact that all three utilize the standard Sorbex bed allotment that enables them to achieve product purities in excess of 98%. The following sechons review each process in detail. [Pg.265]

Remarkably, however, the logarithm of the rate constant varies linearly with the dissociation energy of the allylic C—H bond, which indicates that the rupture of the C—H bond is included in the rate-determining reaction step. Mixed olefin feeds (propene and butene) were also used. It appears that co-dimerization can occur yielding C2 -dimers. [Pg.195]

After separation of the mixed olefins the product work up is similar to that in a steam cracker using LPG feedstock. Small amounts of carbon dioxide are removed and the hydrocarbon gases are dried before passing to a de-ethaniser column. The C2- fraction is passed to an acetylene removal unit before methane is removed from the C2 stream. This comprises 98-i-% ethylene, the remainder being ethane. The C3+ stream is split between the C3 fraction (98% propylene) and C4+. The work up of the C4 stream to produce linear butenes (not shown in the figure) is likely to be less problematic than the corresponding C4 stream from steam crackers, which is highly complex and cannot be separated by fractionation alone. The process produces little product above C5. [Pg.216]

Table VI shows that the tltratable acidity of used acid Is higher and the carbon content lower In the runs containing additives with a 2-butene feed. The difference Is somewhat less but still substantial In the experiments with the mixed olefin feed. For comparison one can estimate the acidity of the blank after feeding 10.6 volumes of olefin/volume acid as 93.2 percent.

Alkylation tests were conducted in the pilot plant with a cat cracker mixed olefin feed. As the water In HF was increased from 0.25 to about 2.8 percent, the alkylate composition changed dramatically. These changes are summarized In Table III detailed alkylate compositions are given In Table VIII. [Pg.43]

HF versus H SO Alkylates. The quality and yield advantages of HF alkylate over H2 0/alkylate made from mixed olefin are attested in the literature (NPRA, 1 3). HF alkylates typically contain higher concen-tratiore of high-octane C0 s and lesser amounts of low-octane C material. Volumetric yields based on olefin feed are generally higher for HF alkylates because of their lower density. [Pg.45]

Marked differences are observed In component distribution of isobo-tane-mixed olefin alkylates prepared with HF and H SO catalysts. The alkylate samples in Table V were prepared under typical operating conditions for the respective processes from similar feedstocks. [Pg.46]

The same effects were seen with mixed olefin feeds. The refinery stream described in Table III was blended with C.P. Grade Isobutane to obtain a 9.0-to-l.O Isobutane-to-olefln molar ratio. This feed was alkylated at temperatures ranging from to 45°C. The contact time was held constant at 1.0 minutes. The results are shown in Table IV. The alkylate compositions include pentanes derived from the feed, but only... [Pg.63]

Two runs were made using the products of first-step reactions in which mixtures of isobutylene and 2-butene had been used. The second-step reactions in such cases resulted in products that were intermediate between those products for runs with pure isobutylene and for runs with pure n-butenes. The RON of the alkylates obtaining using Isobutylene, a 1 1 mixture of Isobutylene and 2-butene, and 2-butene were 89.7, 93.0, and 100.8 respectively. The composition of the TMP family obtained with the mixed olefins also appeared to be Intermediate in nature. [Pg.121]

LASs were found to possess interesting foaming characteristics, which are very significant for their application as detergents. However, LAS can be controlled by foam regulators. Also, the foam produced is stabilized by form stabilizers. The basic processes have been applied for the manufacture of LAS. The dehydrogenation of paraffins, followed by alkylation of benzene with a mixed olefin or paraffin feedstock, represents the most important route for the production of LAS. This process is catalyzed by hydrogen fluoride (HF) [1—4]. [Pg.134]

Conversion of natural gas to liquids is currently of great interest, as many large natural gas fields are not close enough to large markets to make construction of a pipeline economically attractive. These stranded reserves can be liquefied, converted into fuels or converted into (higher value) petrochemicals. U.S. 5,714,662 (to UOP) describes a process for converting crude methanol to olefins. What is the cost of production of the ethylene produced by a plant that produces 900 kmta of mixed olefins if the cost of producing the natural gas feed is 0.5/MMbtu ... [Pg.1155]

Super-Sta-Bac [Reichhold], TM for hydrocarbon resins that are polymers of mixed olefins. [Pg.1196]

Figure 3.35 shows a process flow diagram of Phillips MTBE/ETBE/TAME process. This process is often called the Phillips Etherification Process. The reaction section (1,2) which receives methanol and isobutene concentrate, contains an ion exchange resin. The isobutene concentrate may be mixed olefins from a Fluid Catalytic Cracking Unit (FCCU) or steam cracker or from the on-purpose dehydration of isobutene (Phillips STAR process). High purity MTBE (99 wt%) is removed as a bottoms product from the MTBE fractionator (3). AH of the unreacted methanol is taken overhead, sent to a methanol... [Pg.170]

Sta-Tac . [Arizona] Mixed olefin hydrocarbon resin for adhesives. [Pg.351]

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