Process Engineering and Optimization

Originally appeared in: June 2016, pgs 73-78. Process Engineering Used with permission. and Optimization

T. STREICH, H. KÖMPEL, J. GENG and M. RENGER, thyssenkrupp Industrial Solutions AG, Essen, Germany

Secure the best benefits from C4 hydrocarbon processing—Part 1: Separation sequences

1 Crude C4 streams from the steam coming more and more into focus. n-butenes, another type of very valuable cracker unit (SCU) or the fluidized Different from many conventional C4 components. catalytic cracker unit (FCCU) contain chemical processes, which use pure Different from FCC, steam cracking is a valuable hydrocarbons, such as butadiene chemicals as feedstock, C4 processing thermal cracking method to break down the and C4 olefins. The upgrading of such involves a complex mixture of hydrocarbons C-H bond in light hydrocarbon molecules streams can be carried out with different and other organic/inorganic compounds. to produce hydrogen and olefins. If naphtha processing routes. The upgrading This requires feasible solutions in and/or gasoil are used as feedstock, then process of C4 hydrocarbon streams is not petrochemistry that can only be realized the C4 cut contains about 50% diolefines standardized; a suitable route for each by a tailor-made process design based (mainly 1, 3-butadiene). High-purity 1, refinery must be studied individually. on the individual feedstock to maximize 3-butadiene can be yielded economically Both economic and environmental issues productivity and process economics. with a butadiene extractive distillation should be taken into account to achieve Besides butadiene and butenes, a process. This opportunity is also the main the best investment benefit. considerable portion of butanes are source for 1, 3-butadiene, which is applied Advanced petrochemical plant design included in the C4 cuts from cracker units. in the production of elastomers and co- requires flexibility to match different Furthermore, according to the upstream polymer plastics, such as polybutadiene situations, e.g., variation in feedstock. process, the contaminations contained (e.g., rubber or styrene-butadiene rubber. A comprehensive understanding of C4 traces of solvents, light/heavy hydrocarbons, Beside FCC and SC products, there hydrocarbon processing is prerequisite. C3/C4 acetylene and allenes) can also be exists a multitude of other C4 feedstocks This survey will discuss the characteristics different and must be taken into account derived from blending within a refinery. of C4 feedstocks, as well as the opportunities during the process evaluation. Product Such blended C4 feedstocks also require of the large variety of potential C4 process purification and contaminant removal steps tailor-made processing. routes from a practical engineering point will strongly affect the final profit margin Within this article, the nomenclatures of of view. Some selected technologies will be and increase the plant’s complexity. Raffinate 1 and 2 are used (FIG. 1). After the compared and discussed in more detail. removal of 1, 3-butadiene from crude C4, Feedstock. Crude oil is processed in the residual stream is termed as Raffinate Enhancing the process benefits. petroleum refineries in different ways. In 1, which contains a certain portion of Spurred by the steady growth demand in the field of light olefin production, FCCUs isobutene. Removal of the isobutene, usually light olefins (C2 to C4), the installation of and/or SCUs are utilized. by chemical conversion, leaves Raffinate 2. SCUs and FCCUs—the latter operated An FCCU is used to convert the heavy C4 from field butane (oil carrier gas, natural with catalysts supporting light olefins oil (e.g., vacuum gasoil from crude oil gas or oil shale gas) is a further important formation—has been promoted in vacuum distillation) to gasoline, and it can source for C4 processing. Typical feedstock refineries during the last decades. The be operated in different modes to maximize compositions derived from an SCU, FCCU upgrading of C4 hydrocarbons, one of the middle distillate, gasoline or olefins yield. and field butane are depicted in TABLE 1. most important byproducts in cracker units, The product distribution from an FCCU Crude C4 from an SCU could be more 2 could enhance the benefits of the whole depends on process conditions and catalyst. valuable compared with FCC C4 because process. Many valuable products, such as C4 streams from FCCUs are isobutene- of a higher olefin content. However, the gasoline additives (alkylate, tertiary butyl rich and contain less than 0.5 wt% butadiene. difficulty of separation should not be alcohol, methyl tertiary butyl ether and ethyl However, even a minute portion of butadiene underestimated, and the final economic tertiary butyl ether), monomers for further could cause trouble for downstream benefit has to be evaluated thoroughly with polymerization (butadiene, isobutene, processes, such as catalyst deactivation, respect for the necessary intermediate steps. 1-butene) and commodities (methyl ethyl because of the very active double-bonds or ketone, maleic anhydride), could be yielded potential of polymerization. These small Separation and purification. Upstream from C4 hydrocarbons. Furthermore, the amounts of butadiene cannot be recovered cracking processing generates certain C4 fraction of field butane, such as oil- economically. Selective hydrogenation undesired byproducts. The tailor-made associated gas, natural gas and shale gas, is is the best way to convert butadiene to design of C4 upgrading processes welcomes

HYDROCARBON PROCESSING JUNE 2016 Process Engineering and Optimization flexibilities to fit different feedstocks and typically included in feedstock originating or enhances the distinction in operating cases. In some cases, C4 mixture from cracking processes. Very close boiling volatility between the components, can be established directly as feedstock— points between singular components— will be used, allowing the paraffins/ e.g., FCC C4 cut as feed for alkylation. e.g., 1-butene (–6.3°C) and isobutene olefins molecules to be separated. However, in other cases, butanes-butenes (–6.9°C), and azeotrop formations (as Paraffins leave the column top separation is beneficial or inevitable as in 1-, 3-butadiene and trans-2-butene and solvent with the less-volatile a process step. Product purification is with n-butane)—result in difficulties of components (olefins) flow to the mandatory to fulfill certain specifications separation. Those mixtures are not separable bottom of the distillation column, of downstream chemical synthesis. with conventional distillation methods, and where the extracted components The complexity of a separation/ additional measures are needed. (olefins) are recovered by a purification process strongly depends on The available separation techniques subsequent distillation.5 By adjusting the properties of pure components, as well can be mainly divided into adsorption, the solvent-to-feed ratio, ED as the interactions between components in membrane processing and extractive processes tolerate better fluctuation of the mixture (vapor liquid equilibrium). The distillation. olefin content in feedstock. behavior of fluid mixtures can be calculated • Adsorption, known as molecular Many paraffin/olefin separation by using thermodynamic models, which sieve technology, is a separation processes are based on ED processes, and allow the calculation of these properties from process based on the different the selection of the extractive agent is the available binary experimental data.3 The physical interactions between olefins core know-how of the process design. complexity of determining thermodynamic and adsorbent. It does not need an For instance, a morpholine-based solvent properties is enhanced significantly by additional solvent, but it does require mixture is used in a butene concentration increasing the number of components, a significant amount of electrical process. Such an ED process can be and it is very important to gain the right energy (caused by high product considered as a standalone butane/butene thermodynamic knowledge as a function of circulation rates) and a sophisticated separation, as well as a pretreatment step temperature, pressure and composition. control system. in various synthesis processes for the Due to their better chemical reactivity, • The application of membrane concentration of reactive olefins in the butenes are more valuable than butanes. The processes is very sensible to feedstock feedstock. Pretreatment processes are isolation of butenes from C4 hydrocarbon composition, which contradicts with suitable where the “one-through” conversion streams is profitable, especially for further the diversity of the petrochemical rate is limited by the concentration of use in polymer production. Distillation with process, including varying reactive feed components, such as in the case significant separation effort (stages, reflux feedstocks, since a tight control of of conversion of n-butenes and water to sec- ratio) for separating components with a very byproducts from an FCCU or SCU butanol (SBA). With the implementation close boiling point is a traditional technology is difficult. The low tolerance of feed of an upstream feed concentration unit, the known as super fractionation, and it is used, contaminants would be another recycle stream is reduced (directly reflecting for example, in C2 and C3 olefin/paraffin limitation of membrane techniques on CAPEX) and the operating expense splitters. Due to the larger number of isomers for this industrial application.4 (OPEX) is lowered. in a C4 stream, this system is more complex • The extractive distillation (ED) compared to C2 and C3 processes. process comprises a simpler process Focus on potential C4 processing TABLE 1 shows the normal boiling points setup. A solvent that takes advantage routes. Butadiene as an intermediate (NBP) of C4 components, which are of molecular interaction, and creates product plays a special role in C4 economy. The recovery of butadiene is accomplished TABLE 1. Typical composition of SC C , FCC C and field butane feedstock by using selective solvent via extractive 4 4 distillation. Some features, such as the C4 component NBP, °C SC C4, wt% FCC C4, wt% Field butane, wt% contamination with acetylenes and allenes, 1,3-butadiene –4.4 35–50 0–0.5 – and the risk of self-polymerization, have to Isobutene –6.9 15–30 10–25 – be taken into account in the process design. FIG. 2 shows a typical block flow 2-cis-butene 3.7 5–10 10–20 – diagram of the possible products yielded 2-trans-butene 0.9 5–10 10–20 – from C4 hydrocarbons. However, the 1-butene –6.3 5–20 10–25 – whole scheme would never be applied Isobutane –11.7 1–5 20–40 in its full range. The focus here is on 100 potential opportunities to understand N-butane –0.5 1–10 10–20 the C4 hydrocarbon processing routes. Benchmark scenarios will be discussed SC C4 in accordance with their different process Butadiene Ra nate 1 Isobutene Ra nate 2 complexities. First technical analysis will removal removal FCC C4 be outlined based on evaluation of three border cases. Economic evaluations, including the price development of C process nomenclatures. FIG. 1. 4 feedstocks and products, and handling

HYDROCARBON PROCESSING JUNE 2016 HYDROCARBON PROCESSING JUNE 2016 Process Engineering and Optimization

costs, will be carried out as Part 2 in an purification. As FIG. 3 shows only isobutene co-feedstock isobutane for alkylation, upcoming issue of HP. conversion and further upgrading of the requirements of the gasoline pool, Raffinate 2 to gasoline, an additive will be and the local market demand, including Minimization of capital expenditure taken into account. Butadiene removal is transportation fuel specifications. (Case 1). Usually an olefin containing a only required if butadiene is a problem for C4 stream is too valuable to be used as fuel downstream processes. Maximization of product diversity (via total hydrogenation). In some cases, The upgrading of Raffinate 2 can (Case 2). The main objective of this cutting the mixture into single components be through alkylation, dimerization or case is the maximization of the product is not the goal, so CAPEX can be kept low oligomerization. The process that is best diversity of C4 intermediate products. By due to minimized effort for separation and suited depends on the availability of the tailor-made configuration of the process

Poly-Butadiene Maleic anhydride Alkylates LLDPE TBA Poly- MTBE/ETBE Octene SBA/MEK LDPE PB isobutene

Polymerization Dimerization SBA/MEK Alkylation Polymerization Polymerization synthesis Isobutane 1-Butene 1-Butene

C LPG 2-Butenes 1,3-Butadiene 4 n-Butane 1-Butene 1-Butene Isobutene Isobutane 2-Butenes 1-Butene 2-Butenes Isobutane 2-Butenes

i-/n-Butanes 2-cis/trans 1/2-Butene

butene mixture mixture 1-Butene 1-Butene

1-Butene Isobutene

Isobutane Dehydro-

2-Butenes genation

Distillation n-Butane 2-Butenes 1,3-Butadiene

Butene Distillation Isobutane concentration

1-Butene 1-Butene Isobutane MTBE/ETBE 2-Butenes 2-Butenes n-Butane Distillation TBA backcracking i-/n-Butanes Butene

concentration Isobutene To metathesis Ranate 2 (propylene production) i-/n-Butanes i-/n-Butanes

Butene MTBE/ETBE MTBE Cold acid TBA Hydro- hydrogenation synthesis backcracking isobutene removal synthesis isomerization

Ranate 1

1,3-Butadiene 1,3-Butadiene Selective Isobutane extractive Isomerization distillation hydrogenation

i-/n-Butanes C4-fraction C4-fraction C4-fraction ﬁeld butane steam cracker FCC i-/n-Butanes

FIG. 2. Block flow diagram of process routes for the separation and conversion of C4 hydrocarbons.

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steps, it is possible to isolate almost all C4 Isobutene is used for polymerization 1-/2-butenes and n-/iso butanes. The linear components derived from an SC/FCC to polyisobutene or butyl rubber; for olefin 1-butene is a desired feedstock for stream. Only cis/trans-isomers of 2-butene methyl tert-butyl ether (MTBE)/ethyl the production of n-butene polyolefines, will remain as a mixture. By applying tert-butyl ether (ETBE) synthesis; and for as co-monomer in the production of polymerization, dimerization, metathesis, tertiary butyl alcohol (TBA) synthesis. polyethylene—low-density polyethylene oxidation, alkylation, hydration and For isobutene isolation as an intermediate (LDPE) and high-density polyethylene etherification, these components can be product with high purity, isobutene can be (HDPE)—or as feedstock for propylene further processed to high-value products. converted to ether (MTBE/ETBE) or to synthesis via metathesis of ethylene and 6 FIG. 4 represents the link between C4 TBA via direct hydration. Crude TBA can butene. The recovery of 1-butene from intermediates and high-value products. be sold as TBA/water azeotrope or further the cracker-mixed C4 stream is difficult due With the removal of butadiene via treated to pure TBA (>99.9 wt%) by drying to stringent limitations for isobutene and extraction or selective hydrogenation, the steps. Alternatively, the azeotropic mixture butadiene in 1-butene product (TABLE 2).7 cracker stream is converted to Raffinate 1. can be decomposed to high-purity isobutene Such separation can be accomplished It is then routed to isobutene processing (99.98 wt%) at temperatures below 150°C by processing the Raffinate 2 stream in a where isobutene is removed by chemical and moderate pressure with heterogeneous two-step super fractionation. In the first reaction from 1-butene (a nearly identical catalyst.6 Etherification and TBA synthesis distillation column, 2-cis/trans-butene boiling point) and the other butene and are highly selective to isobutene, due to the and n-butane form the bottom product, butane components. Besides isobutene, inert behavior of all other C4 components at whereas 1-butene and isobutane go four further products can be derived from such mild reaction conditions. overhead and are separated in the second Raffinate 1: 1-butene, 2-butene (cis/ By isobutene removal, Raffinate 1 is column. Isobutane, along with some trans), isobutane and n-butane. transferred into Raffinate 2 containing 1-butene, is recovered as overhead product and high-purity 1-butene forms the Butadiene Crude C4 Ranate 1 Isobutene Ranate 2 Ranate II bottom product. Isobutane can be further removal conversion Gasoline pool (optional) upgrading used to produce alkylates via alkylation or tertiary butyl hydroperoxid via oxidation. The bottom product of the first column MTBE or ETBE or TBA of 1-butene separation consists mainly of n-butane and 2-cis/trans-butene. By using FIG. 3. C process route for minimized CAPEX for C processing. the butene concentration process, as shown 4 4 FIG. 4, 2-butene can be separated from n-butane. The above mentioned process C4-fraction C4-fraction FCC steam cracker TABLE 2. Composition of high-purity isobutene and 1-butene 1,3-Butadiene 1,3-Butadiene Polymerization Synthetic Isobutene rubber Isobutane Component Pure isobutene Pure 1-butene N-Butane 1-Butene Alkylation Alkylates Isobutene 99.98 wt% 0.15 2-Butene (c/t) Isobutane 1-butene 0.005 wt% 99.7 Oxidation Tertiary butyl Butadiene Butadiene hydro peroxide selective extractive- 2-butene 0.01 wt% 0.01 hydrogenation distillation Oxidation Maleic Butane 0.005 wt% 0.15 n-Butane anhydride Ranate-1: 1, 3-butadiene < 10 ppm < 10 ppm Isobutene Isobutane Oxidation Isobutane Octene TBA < 5 ppm < 1 ppm N-Butane 1-Butene Distillation 1-Butene Dimerization Water < 30 ppm < 10 ppm 2-Butene (c/t) Sulfur < 1 ppm < 1 ppm Isobutene Ranate-2: Polybutylene Polymerization reaction Isobutane Distillation 1-Butene (to TBA or MTBE) N-Butane 1-Butene LDPE/LLDPE 1-Butene Ranate 2 2-Butene (c/t) SBA N-Butane n-Butane

T-2-Butene C-2-Butene Hydration

TBA or MTBE Isobutene Isobutane Butene MEK concentration T-2-Butene 2-Butene Metathesis Propylene TBA N-Butane C-2-Butene (trans+cis) Ranate 1 MTBE or TBA MTBE 1-Butene Polymerization Polyisobutylene TBA or MTBE Isobutene ETBE 2-butene backcracking Copolymerization Butyl rubber with isoprene FIG. 5. Raffinate 1 and Raffinate 2 secondary

FIG. 4. C4 intermediate products and corresponding final products. products.

HYDROCARBON PROCESSING JUNE 2016 HYDROCARBON PROCESSING JUNE 2016 Process Engineering and Optimization

route has an advantage compared to the the production of SBA and/or MEK. (C2–C4), resulting in small amounts conventional process route whereas 1- and A mixture of isobutane and n-butane of propylene and C4 byproducts. As 2-butenes are still in the feedstock. Due to derived from butene concentration can be compensation, propylene and butene on- the fact that 1-butene was already removed, sold as a liquefied petroleum gas (LPG) purpose technologies have been developed. the butene concentration unit can be operated more economically compared to using Raffinate 2 The upgrading process of C4 hydrocarbon streams feedstock, including 1/2-butenes. is not standardized; a suitable route for each N-butane can be further processed to maleic anhydride by oxidation refinery must be studied individually. Economic and with air. 2-butene (-cis/trans) is environmental issues should be taken into account forwarded to SBA/methyl ethane ketone (MEK) synthesis, which to achieve the best investment benefit. will be outlined in the next section. Within Case 2, five C4 intermediate products and three final product. Within the SBA synthesis, all three Field C4 that is separated from natural products can be processed, beginning with species of butenes form SBA. The variation gas, oil associated gas or shale gas contains Raffinate 1 (FIG. 5). of feedstock with regard to ratio of 1-butene mainly butanes and no butenes. Butene and 2-butenes (cis/trans) will have no yielded from such butane feedstock by Maximize single product yields significant impact on process design; hence, dehydrogenation can also be applied in every (Case 3). In this case, the focus is on a separation of 1-butene is not considered. butene upgrading processes discussed above, the maximization of one final product A block flow diagram for the SBA/MEK and is particularly suitable for a process with based on C4 intermediates. As an production is shown in FIG. 7. a high requirement on feedstock quality. example, MEK, which is derived from Dehydrogenation is an endothermic sec-butanol (SBA), is chosen (FIG. 6). Processing field butanes. The change in equilibrium reaction, usually operating in The challenge is to minimize byproducts the availability of feedstocks over the years is the vapor phase. The paraffin conversion and to meet the feedstock specification driving the development of petrochemical increases with decreasing pressure and for SBA/MEK synthesis (TABLE 3). A technologies. In the last decades, ethylene increasing temperature. Obviously, further objective of this processing route plants/SCUs were often built as gas crackers conversion is limited by the thermodynamic is to maximize the 1-butene/2-butene Isobutane concentration of feedstock for SBA/ Butadiene Ranate 1: Isobutene Ranate 2: N-Butane C4 fraction selective reaction Butane LPG MEK synthesis up to 97 wt%. FCC hydrogenation Isobutene (to TBA or MTBE) Isobutene concentration Technology used for the SBA synthesis Isobutane Isobutane SC/FCC-product: N-Butane N-Butane is a direct hydration process of 1/2-butenes 1,3-Butadiene 1-Butene 1-Butene 1-Butene T-2-Butene in the presence of sulfonic cation exchange Isobutene 2-Butene (cis/trans) 2-Butene (c/t) C-2-Butene Isobutane resin in the water phase, and the subsequent N-Butane SBA C4 gas separation from the raw SBA. Of the 1-Butene synthesis bulk of the SBA produced worldwide, over 2-Butene (cis/trans) SBA SBA 90% is utilized as an intermediate for the Butadiene MEK C4-fraction extractive MEK manufacturing of MEK. MEK is mainly synthesis steam cracker distillation utilized as a solvent in paints, lacquers TBA or MTBE and printing inks, as well as an extraction MTBE or TBA solvent in several industrial sectors (e.g., 1,3-Butadiene lube oil, plastics and rubber). 1,3-Butadiene Polymerization Synthetic rubber With regards to byproducts, SC and FCC feedstocks have to be differentiated. FIG. 6. Processing route for the maximization of single-selected product MEK and minimum Where an FCC feedstock is available, byproducts. small contents of 1, 3-butadienes will be removed by selective hydrogenation. Butenes feed In the case of SC feedstock, it is recommended to extract 1, 3-butadienes SBA Raw SBA SBA Pure SBA MEK Raw MEK MEK MEK due to a much higher concentration. A synthesis 97 wt-% distillation 99 wt-% synthesis 78 wt-% distillation >99.7 wt-% summary of this specification is given TABLE 3. in The limitation for isobutene Pure SBA as product is important to prevent formation of additional TBA during SBA synthesis. 99 wt-% A butene concentration unit Raw TBA (pretreatment) is able to provide a tailor- made feedstock, which can be used for FIG. 7. Block diagram of SBA/MEK synthesis and purification.

HYDROCARBON PROCESSING JUNE 2016 HYDROCARBON PROCESSING JUNE 2016 Process Engineering and Optimization

4 Hydration TBA Eldridge, R. B., “Olefin/paraffin separation technology: A review,” Industrial & Engineering Isobutane Dehydrogenation Isobutene Polymerization Polyisobutylene Chemistry Research, 1993. 5 Emmrich G., H. Gehrke and U. Ranke, “Working Field C4 Etheriﬁcation MTBE/ETBE with an extractive distillation process,” Krupp Uhde Oil associated Isomerization GmbH, 2001. gas, natural 6 (optional) Schulze, J., and M. Homann, C4-hydrocarbons and gas, shale gas Distillation Metathesis Propylene derivatives, Springer-Verlag, 1989. 7 Edwards, S. M., S. J. Stanly and M. Shreehan, “Relative economics of mixed C processing routes,” Dehydrogenation N-butene Polymerization Polyisobutylene 4 n-Butane ABB Lummus Global, 1998. Co-polymerization LLDPE DR. THOMAS STREICH is the head of the refining and petrochemical FIG. 8. Processing lines and corresponding products based on field butane. division at thyssenkrupp Uhde Engineering Services GmbH, Germany. He has over 25 years of TABLE 3. Typical specifications for n- reasons behind this indicate the wide engineering and research and butenes feed within SBA/MEK synthesis diversities of product spectrum and the development (R&D) experience in possibilities of blending inside of refineries. the fields of refining, hydrocarbon and petrochemical Component Composition processing, with a special focus on C /C production Meaningful economic evaluation is therefore 3 4 Isobutene Max. 0.7 wt% technologies. Dr. Streich holds two degrees in based on the proper understanding and constructional design and process engineering, N-butane as well as a doctorate degree in chemical engineering Residual comparison of possible processing routes. Isobutane A simple way for upgrading from the Ruhr-University of Bochum in Germany. 1-butene C4 hydrocarbons with minimized HARALD KÖMPEL is the deputy 2-cis-butene Min. 97 wt% intermediate steps can result in high head of the refining, petrochemical and technologies department at 2-trans-butene octane gasoline components. As a second extreme, the maximization of intermediate thyssenkrupp Uhde Engineering 1,3-butadiene Max. 0.4 wt% Services GmbH, Germany. He has steps to separate the crude C4 mixture into 26 years of experience in the fields MTBE single components for further upgrading of refining, hydrocarbon and MeOH Max. 0.2 wt% by chemical synthesis has been reviewed. petrochemical processing, with a focus on light olefins and their downstream products, including H2O There is a route with special reflection on the successful commercialization of the methanol to one selected chemical synthesis, MEK. propylene (MTP) process. Mr. Kömpel holds a degree in chemical engineering from the Friedrich Alexander equilibrium and requires a recycle of Butenes from field C4 via dehydrogenation unreacted paraffins. Separation and could cover the gap of high-purity University Erlangen-Nuremberg. purification yielding in high-purity butene butene requirements for certain special JIN GENG is a process engineer/ is mandatory for the process. Generally, applications, e.g., polymerization. technologist in the refining, the hydrogen and light hydrocarbons that Based on the technical possibilities petrochemicals and technologies department at thyssenkrupp are the byproducts of dehydrogenation can discussed here, a full economic evaluation Uhde Engineering Services GmbH, be removed by distillation. will be carried out in a follow-up part to Germany. He earned an MS degree Either n-butene or isobutene could be this publication. Depending on the feed in chemical engineering with the focus on separation science and thermodynamics produced with the butane dehydrogenation composition, a tailor-made process route from the Friedrich Alexander University Erlangen- process. FIG. 8 shows the product lines should be chosen to get the best benefit Nuremberg. He has recently exhibited his doctor based on field butane. Owing to the high from case to case. thesis at the same university. quality of butenes, polymerization would Next month. MATTHIAS RENGER is a senior prove to be very beneficial to upgrading. Part 2 of this article will process engineer within the appear in July. refining, petrochemical and Overview and outlook. A comprehensive technologies department at overview on C olefin/paraffin-processing LITERATURE CITED thyssenkrupp Uhde Engineering 4 1 Bender, M., “An overview of industrial processes Services GmbH, Germany. He has and the features of the crude C4 feedstocks, for the production of olefins—C4 hydrocarbons,” over 7 years of experience in as well as possible product lines, have been ChemBioEng Reviews, 2014. process modelling and the design of chemical discussed. Engineering companies in 2 Sadeghbeigi, R., Fluid Catalytic Cracking Handbook, processes, including process design packages and petrochemical industries must steadily face Butterworth-Heinemann, 2012. studies, basic engineering, and commissioning, 3 Gmehling, J., D. D. Liu and J. M. Prausnitz, “High- operation and troubleshooting. He holds a degree in the challenge that the available feedstock pressure vapour-liquid equilibria for mixtures power and process engineering from the Berlin will somehow depart from the “desired” containing one or more polar components,” Institute of Technology (TU Berlin, Germany). compositions and specifications. The Chemical Engineering Science, 1979.

thyssenkrupp Uhde Engineering Services GmbH Friedrich-Uhde-Str. 2 • 65812 Bad Soden/Taunus • Germany Contact person: Dr. Thomas Streich • Phone: +49 6196 205-1750 • [email protected] www.thyssenkrupp-industrial-solutions.com