Patent Application
20130165712
This application claims the benefit of European Patent Application No. 11195827.8, filed Dec. 27, 2011, the entire disclosure of which is hereby incorporated by reference.
The invention relates to an integrated process for preparing ethylene and/or other lower olefins.
Oxygenate-to-olefin processes are well described in the art. Typically, oxygenate-to-olefin processes are used to produce predominantly ethylene and propylene. An example of such an oxygenate-to-olefin process is described in U.S. Patent Application Publication No. 2011/112344, which is herein incorporated by reference. The publication describes a process for the preparation of an olefin product comprising ethylene and/or propylene, comprising a step of converting an oxygenate feedstock in an oxygenate-to-olefins conversion system, comprising a reaction zone in which an oxygenate feedstock is contacted with an oxygenate conversion catalyst under oxygenate conversion conditions, to obtain a conversion effluent comprising ethylene and/or propylene.
The publication further describes possible integration with a cracker. The publication also describes partially hydrogenating a C4 portion of the conversion effluent and/or cracker effluent and recycling at least part of the at least partially hydrogenated C4 as recycle feedstock to the cracker or oxygenate-to-olefins conversion system.
As market conditions change quite frequently, flexibility of a process system is important to its viability. This is especially important to a process that is integrated with other processes that provide feeds to the process or take outputs from the process. For example, in an oxygenate-to-olefin process, it is beneficial to be able to flexibly adjust the amount of each of the different products produced by the process. In addition, this process is typically integrated with other units so it is important to keep the feed supply constant even when product demand changes.
The invention provides a process for the preparation of an olefin product comprising ethylene, which process comprises the steps of: a) cracking a cracker feedstock under cracking conditions in a cracking zone to obtain a cracker effluent comprising olefins; b) converting an oxygenate feedstock in an oxygenate-to-olefins conversion system, comprising a reaction zone in which an oxygenate feedstock is contacted with an oxygenate conversion catalyst under oxygenate conversion conditions, to obtain a conversion effluent comprising ethylene and/or propylene; c) combining at least part of the cracker effluent and at least part of the conversion effluent to obtain a combined effluent wherein the combined effluent comprises a C4 portion and a C3 portion; d) separating at least a part of the C3 portion from the combined effluent to form a combined propylene stream; e) separating at least a part of the C4 portion from the combined effluent to form a C4 stream; and f) recycling at least a part of the combined propylene stream as recycled propylene to step b).
Reference is made to
The process comprises an oxygenate-to-olefins (OTO) conversion system 8; a cracking system 5, also referred to as cracker 5; and a work-up section 60. An oxygenate feedstock is fed via line 15 to the OTO conversion system 8, for example, comprising methanol and/or dimethylether. Optionally, a hydrocarbon stream and/or a diluent are fed to the OTO conversion system via lines 17 or 19, respectively. A cracker feedstock is fed via line 10 to the steam cracker 5. Water or steam is also fed to the cracker 5 as a diluent via line 12.
In one embodiment, the cracker is an ethane cracker, and the cracker feedstock is an ethane-comprising feedstock. The feedstock preferably comprises at least 50 wt % ethane, more preferably at least 60 wt % and most preferably at least 70 wt % ethane. The use of an ethane-rich feedstock maximizes the ethylene production from the cracker.
In another embodiment, the cracker is a naphtha, gas oil, hydrowax or vacuum gas oil cracker. Alternatively, the cracker feedstock may be any combination of these or heavier and/or lighter components. The feed to the cracker will in large part determine the composition of the cracker effluent.
In principle every known OTO conversion system and process can be used in conjunction with the present invention, including processes known as Methanol-to-Olefins (MtO) and Methanol to Propylene (MtP). The OTO conversion system and process can for example be as disclosed in U.S. 2005/0038304, incorporated herein by reference; as disclosed in U.S. 2010/206771, incorporated herein by reference; or as disclosed in U.S. 2006/020155 incorporated herein by reference. Other particularly suitable OTO conversion processes and systems with specific advantages are disclosed in U.S. 2009/187058, U.S. 2010/298619, U.S. 2010/268009, U.S. 2010/268007, U.S. 2010/261943, and U.S. 2011/160509, all of which are herein incorporated by reference.
In one embodiment, molecular sieve catalysts are used to convert oxygenate compounds to light olefins. Silicoaluminophosphate (SAPO) molecular sieve catalyst may be used that are selective to the formation of ethylene and propylene. Preferred SAPO catalysts are SAPO-17, SAPO-18, SAPO-34, SAPO-35, SAPO-44, the substituted forms thereof and mixtures thereof. The oxygenate feedstock may comprise one or more aliphatic containing compounds, including alcohols, amines, carbonyl compounds, for example, aldehydes, ketones and carboxylic acids, ethers, halides, mercaptans, sulfides, and the like and mixtures thereof. Examples of suitable feedstocks include methanol, ethanol, methyl mercaptan, ethyl mercaptan, methyl sulfide, methyl amine, di-methyl ether, di-ethyl ether, methyl ethyl ether, methyl chloride, ethyl chloride, dimethyl ketone, formaldehyde, acetaldehyde and various acids such as acetic acid.
In one embodiment, the oxygenate feedstock comprises one or more alcohols having from 1 to 4 carbon atoms and most preferably methanol. The oxygenate feedstock is contacted with a molecular sieve catalyst and is converted to light olefins, preferably ethylene and propylene.
Preferably, the OTO conversion system is arranged to receive an olefin stream, and is able to at least partially convert this stream, in particular a stream comprising C4 olefins, to ethylene and/or propylene. In one embodiment, the olefin can be contacted with the oxygenate conversion catalyst in the OTO reaction zone; see for example WO 2009/039948, WO 2007/135052, WO 2009/065848 and WO 2009/065877. The oxygenate conversion catalyst preferably comprises an aluminosilicate, in particular a zeolite.
In one embodiment, an olefinic co-feed is fed to the oxygenate-to-olefins conversion system. An olefinic co-feed is a feed containing one or more olefins or a mixture of olefins. The olefinic co-feed may also comprise other hydrocarbon compounds, for example, paraffinic compounds, alkylaromatic compounds, aromatic compounds or mixtures thereof. The olefinic co-feed preferably comprises more than 25 wt % olefins, more preferably more than 50 wt %, still more preferably more than 80 wt % and most preferably in the range of from 95 to 100 wt % olefins. A preferred olefinic co-feed consists essentially of olefins. Non-olefinic compounds in the olefinic co-feed are preferably paraffinic compounds. The olefins in the olefinic co-feed are preferably mono-olefins. Further, the olefins can be linear, branched or cyclic, but they are preferably linear or branched. The olefins may have from 2 to 12 carbon atoms, preferably 3 to 10 carbon atoms and more preferably from 3 to 8 carbon atoms.
In another embodiment, the OTO conversion system comprises an olefin cracking zone downstream from the OTO reaction zone and is arranged to crack C4+ olefins produced in the OTO reaction zone, as described in U.S. Pat. No. 6,809,227 and U.S. 2004/0102667, incorporated herein by reference. In one embodiment, the olefin produced in the OTO conversion system is fed to the olefin cracking zone.
In one embodiment, the yield of light olefins can be increased by converting the fraction that is heavier than propane to lighter olefins in an olefin cracking unit. The olefin cracking unit may use any molecular sieve catalyst capable of converting hydrocarbons with 4 or more carbon atoms into light olefins. Preferred molecular sieve catalysts for this olefin cracking unit are SAPO and zeolites as described hereinafter. The most preferred catalyst for this olefin cracking unit is ZSM-5.
Both the OTO process and the optional catalytic olefin cracking process may be operated in a fluidized bed or moving bed, e.g. a fast fluidized bed or a riser reactor system, and also in a fixed bed reactor or a tubular reactor. A fluidized bed or moving bed, e.g. a fast fluidized bed or a riser reactor system are preferred.
In the steam cracker 5, the cracker feedstock is cracked under cracking conditions to produce a cracker effluent comprising lower olefins in line 22.
Catalysts suitable for converting the oxygenate feedstock preferably include molecular sieve-comprising catalyst compositions. Such molecular sieve-comprising catalyst compositions typically also include binder materials, matrix material and optionally fillers. Suitable matrix materials include clays, such as kaolin. Suitable binder materials include silica, alumina, silica-alumina, titania and zirconia, wherein silica is preferred due to its low acidity.
Molecular sieves preferably have a molecular framework of one, preferably two or more corner-sharing [TO4] tetrahedral units, more preferably, two or more [SiO4], [AlO4] and/or [PO4] tetrahedral units. These silicon, aluminum and/or phosphorus based molecular sieves and metal containing silicon, aluminum and/or phosphorus based molecular sieves have been described in detail in numerous publications including for example, U.S. Pat. No. 4,567,029. In a preferred embodiment, the molecular sieves have 8-, 10- or 12-ring structures and an average pore size in the range of from about 3 Å to 15 Å.
Suitable molecular sieves are silicoaluminophosphates (SAPO), such as SAPO-17, -18, 34, -35, -44, but also SAPO-5, -8, -11, -20, -31, -36, 37, -40, -41, -42, -47 and -56; aluminophosphates (AlPO) and metal substituted (silico)aluminophosphates (MeAlPO), wherein the Me in MeAlPO refers to a substituted metal atom, including metal selected from one of Group IA, IIA, IB, IIIB, IVB, VB, VIB, VIIB, VIIIB and Lanthanide's of the Periodic Table of Elements, preferably Me is selected from one of the group consisting of Co, Cr, Cu, Fe, Ga, Ge, Mg, Mn, Ni, Sn, Ti, Zn and Zr.
Alternatively, the conversion of the oxygenate feedstock may be accomplished by the use of an aluminosilicate-comprising catalyst, in particular a zeolite-comprising catalyst. Suitable catalysts include those containing a zeolite of the ZSM group, in particular of the MFI type, such as ZSM-5, the MTT type, such as ZSM-23, the TON type, such as ZSM-22, the MEL type, such as ZSM-11, the FER type. Other suitable zeolites are for example zeolites of the STF-type, such as SSZ-35, the SFF type, such as SSZ-44 and the EU-2 type, such as ZSM-48.
Aluminosilicate-comprising catalysts, and in particular zeolite-comprising catalysts, have the additional advantage that in addition to the conversion of methanol or ethanol, these catalysts also induce the conversion of olefins to ethylene and/or propylene. Furthermore, these aluminosilicate-comprising catalysts, and in particular zeolite-comprising catalysts, are particularly suitable for use as the catalyst in a catalytic olefin cracking zone. Particular preferred catalyst for this reaction, i.e. converting part of the olefins in the olefinic product, are catalysts comprising at least one zeolite selected from MFI, MEL, TON and MTT type zeolites, more preferably at least one of ZSM-5, ZSM-11, ZSM-22 and ZSM-23 zeolites.
In one preferred embodiment, the molecular sieve in the molecular sieve-comprising catalyst is a non-zeolitic molecular sieve, while part of the olefinic product, in particular at least part of the C4+ fraction containing olefins, is provided to a subsequent separate catalytic olefin cracking zone with a zeolite-comprising catalyst and the C4+ hydrocarbon fraction is at least partially converted by contact with the zeolite-comprising catalyst.
Preferred catalysts, for both the OTO reaction as well as an optional catalytic olefin cracking reaction, comprise a more-dimensional zeolite, in particular of the MFI type, more in particular ZSM-5, or of the MEL type, such as zeolite ZSM-11. Such zeolites are particularly suitable for converting olefins, including iso-olefins, to ethylene and/or propylene. The zeolite having more-dimensional channels has intersecting channels in at least two directions. So, for example, the channel structure is formed of substantially parallel channels in a first direction, and substantially parallel channels in a second direction, wherein channels in the first and second directions intersect. Intersections with a further channel type are also possible. Preferably the channels in at least one of the directions are 10-membered ring channels. A preferred MFI-type zeolite has a Silica-to-Alumina ratio SAR of at least 60, preferably at least 80.
Particular catalysts, for both the OTO reaction as well as an optional olefin cracking reaction, include catalysts comprising one or more zeolite having one-dimensional 10-membered ring channels, i.e. one-dimensional 10-membered ring channels, which are not intersected by other channels. Preferred examples are zeolites of the MTT and/or TON type. Preferably, the catalyst comprises at least 40 wt %, preferably at least 50% wt of such zeolites based on total zeolites in the catalyst.
In a particularly preferred embodiment the catalyst, for both the OTO reaction as well as an optional catalytic olefin cracking reaction, comprises in addition to one or more one-dimensional zeolites having 10-membered ring channels, such as of the MTT and/or TON type, a more-dimensional zeolite, in particular of the MFI type, more in particular ZSM-5, or of the MEL type, such as zeolite ZSM-11.
The catalyst, for both the OTO reaction as well as an optional catalytic olefin cracking reaction, may comprise phosphorus as such or in a compound, i.e. phosphorus other than any phosphorus included in the framework of the molecular sieve. It is preferred that an MEL or MFI-type zeolites comprising catalyst additionally comprises phosphorus. The phosphorus may be introduced by pre-treating the MEL or MFI-type zeolites prior to formulating the catalyst and/or by post-treating the formulated catalyst comprising the MEL or MFI-type zeolites. Preferably, the catalyst comprising MEL or MFI-type zeolites comprises phosphorus as such or in a compound in an elemental amount of from 0.05-10 wt % based on the weight of the formulated catalyst. A particularly preferred catalyst comprises MEL or MFI-type zeolites having SAR of in the range of from 60 to 150, more preferably of from 80 to 100, and phosphorus, wherein the phosphorus has preferably been introduced by post-treatment of the formulated catalyst. An even more particularly preferred catalyst comprises ZSM-5 having SAR of in the range of from 60 to 150, more preferably of from 80 to 100, and phosphorus, wherein the phosphorus has preferably been introduced by post-treatment of the formulated catalyst. The phosphorus may be introduced by impregnation of the zeolite with phosphoric acid, which is typically followed by calcination at 550° C.
It is preferred that molecular sieves in the hydrogen form are used in the oxygenate conversion catalyst in step (g), e.g., HZSM-22, HZSM-23, and HZSM-48, HZSM-5. Preferably at least 50 wt %, more preferably at least 90 wt %, still more preferably at least 95 wt % and most preferably 100 w % of the total amount of molecular sieve used is in the hydrogen form. It is well known in the art how to produce such molecular sieves in the hydrogen form.
Typically the catalyst deactivates in the course of the process, primarily due to deposition of coke on the catalyst. Conventional catalyst regeneration techniques can be employed to remove the coke. It is not necessary to remove all the coke from the catalyst as it is believed that a small amount of residual coke may enhance the catalyst performance and additionally, it is believed that complete removal of the coke may also lead to degradation of the molecular sieve. This applies to the catalyst for both the OTO reaction as well as an optional catalytic olefin cracking reaction.
The catalyst particles used in the process of the present invention can have any shape known to the skilled person to be suitable for this purpose, for it can be present in the form of spray dried catalyst particles, spheres, tablets, rings, extrudates, etc. Extruded catalysts can be applied in various shapes, such as, cylinders and trilobes. If desired, spent oxygenate conversion catalyst can be regenerated and recycled to the process of the invention. Spray-dried particles allowing use in a fluidized bed or riser reactor system are preferred. Spherical particles are normally obtained by spray drying. Preferably the average particle size is in the range of 1-200 μm, preferably 50-100 μm.
Suitable OTO processes will be further described in detail below. In the OTO conversion system 8, the oxygenate feedstock, and optionally an olefin co-feed (which can be partly or fully a recycle stream) are contacted with an oxygenate conversion catalyst under oxygenate conversion conditions, to obtain a conversion effluent comprising lower olefins in line 25. An optional diluent stream may comprise water, steam, inert gases such as nitrogen and/or paraffins, such as methane.
The reaction conditions of the oxygenate conversion include a reaction temperature of 350 to 1000° C., preferably from 350 to 750° C., more preferably 450 to 700° C., even more preferably 500 to 650° C.; and a pressure from 0.1 kPa (1 mbar) to 5 MPa (50 bar), preferably from 100 kPa (1 bar) to 1.5 MPa (15 bar).
Effluents from the cracking and OTO conversion system need to be worked up in order to separate and purify various components as desired, and in particular to separate one or more lower olefin product streams.
Typically, in known steam cracker processes as well as OTO processes, the effluent is quenched in a quench unit with a quench medium such as water to cool the process gas before feeding it to a compressor. This allows for a smaller compressor and lower power consumption due to reduced gas volume. Any liquid hydrocarbons after the quench are phase separated from liquid water and separately recovered. The water or steam recovered from the quench unit can be partially recycled as diluent to the OTO conversion system via line 19 or to the cracker via line 12. The water may first be treated or purified, for example, to remove catalyst fines.
The vapor components after the quench are typically sent to a compression section that can comprise multiple compression steps, subjected to a caustic wash treatment, dried and sent to a separation including a cold section, to obtain separate streams of the main components. Additional compression steps may be carried out during, or after any of the above mentioned washing and drying steps.
It will be understood that cracker and conversion effluents can be combined at various stages of work-up, such as before quenching, after quench and before compression, or after compression. In addition, the effluents can be combined before or after a caustic wash tower or at different stages of the product separation downstream of the compression section.
It is advantageous to recycle at least part of the various streams to the OTO conversion system 8. The process of this invention comprises recycling at least a portion of the combined propylene from the combined cracker and OTO conversion system to the OTO conversion system. By recycling the propylene to the OTO conversion system, the amount of C4, C5 and C6 olefins produced will increase. This is especially beneficial if demand for propylene is reduced, i.e., when a downstream polypropylene plant is offline.
This allows the plant to continue to operate at desired feed rates without producing excess propylene which is difficult to store. By maintaining feed rates, the upstream and other downstream units can continue to operate at desired feed rates without having to divert feeds or products to intermediate storage facilities. For example, an upstream unit producing methanol from methane can continue operating at normal rates even when the propylene outlet is constrained. Additionally, it is easier to store and/or transport C4+ olefins than C3 olefins so shifting of production from propylene to heavier olefins can be useful in certain situations.
Cracker units are typically operated to reduce the amount of propylene recycled to the cracker furnace at the expense of naphtha or LPG feed. By integrating with an OTO conversion system, the propylene can be recycled to the OTO unit instead of sending it to the cracker furnace where it would replace cracker feed and result in a lower production of C4+ material from the cracker. Additionally, this results in the propylene being converted more selectively to C2 and/or C4 olefins.
Some changes may be necessary to allow the system to handle the recycle of a portion of or the entire propylene stream. Feeding propylene to the OTO reactor may require additional steam to be fed to the OTO reactor as diluent. Further, depending on the reactor capacity available, the recycle of propylene may result in a decrease in the allowable feed rate of one or more other feed components, for example, the oxygenate feedstock or olefin feed stream may need to be reduced to accommodate the propylene recycle.
In one embodiment, furnaces associated with the OTO conversion system need to be taken off-line for decoking. The ethane or other component that is normally fed to the furnace can temporarily be recycled to the OTO conversion system. During this time, the ethane or other component will begin to build up in the process, although the process is still producing ethylene and other products. When the furnace is brought back on-line, the ethane can be withdrawn from the process and fed to the furnace. This results in a reduced need for spare furnaces.
Although
The amount of recycled propylene to the OTO conversion system is at least 3 wt %, calculated as the total feed to the OTO conversion system. The amount of recycled propylene is preferably at least 5 wt %, more preferably at least 10 wt % and most preferably at least 15 wt %. The stream comprising the recycled propylene is preferably at least 60 wt % olefinic, more preferably at least 90 wt % olefinic and most preferably at least 99 wt % olefinic.
Typically, both the steam cracker effluent and the OTO conversion system effluent will contain C4 species, in particular including unsaturated C4 species. The cracker effluent will typically contain more butadiene than the conversion effluent of the OTO conversion system. The effluents from both the cracker and the OTO conversion typically contain butene and a quantity of butane.
In one particular embodiment, the stream 44 comprises a significant quantity of di-olefins, in particular butadiene. A significant quantity of butadiene is for example, at least 0.1 wt % of butadiene in the stream, in particular at least 0.5 wt %, more in particular at least 1 wt %, or at least 2 wt %. The stream comprising a significant quantity of butadiene may be subjected to selective hydrogenation conditions in hydrogenation unit 54 to convert butadiene to butene, while preferably minimizing the hydrogenation of butene to butane.
A suitable process for selective hydrogenation is described in U.S. Pat. No. 4,695,560. It is preferred for at least 90 wt % of the butadiene to be converted to butene and less than 10 wt %, preferably less than 5 wt % of the butene to be converted to butane.
In another embodiment, the butadiene is removed through extractive distillation using polar extractive distillation solvents, for example, acetonitrile, N-formylmorpholine, and/or dimethylformamide. The extractive distillation process produces a butadiene stream and a remaining C4 stream which comprises C4 mono-olefins and C4 alkanes.
The effluent from selective hydrogenation is a C4 feedstock comprising butene, and butene is a desirable co-feed in OTO reactions, in particular in a process in which a catalyst comprising an aluminosilicate or zeolite having one-dimensional 10-membered ring channels and an olefin co-feed is employed. The butene rich effluent can be recycled via line 57b.
In the OTO process, some paraffins are formed, for example C4 saturates that will build up in the system until they are removed. An optional bleed line is present to remove these paraffins from the system.
In one embodiment, the C5 and/or C6 olefin streams may be recycled to the OTO reactor. In another embodiment, the C5 and/or C6 streams may be fed to an olefin cracking unit where the olefins are cracked to lower olefins, preferably ethylene and propylene. Any propylene formed in the olefin cracking unit may also be recycled to the OTO conversion system.
The propylene may be fed to an olefin cracking unit, but it is preferably fed to the OTO conversion system to make additional ethylene and C4+ olefins. As can be seen from the examples, it is preferred to recycle propylene to the OTO conversion system. The conversion of propylene fed to an olefin cracking unit is very low so recycling propylene to the olefin cracking unit is not preferred.
In another embodiment, stream 44 comprising unsaturated C4 species is subjected to more severe hydrogenation conditions in unit 54 so that butenes as well as any butadiene are substantially fully hydrogenated, and an effluent rich in butane is obtained in line 56.
Such a butane-rich stream can be recycled as feedstock to the steam cracker 5 via line 57a to produce additional ethylene.
Two catalysts, comprising 40 wt % zeolite, 36 wt % kaolin and 24 wt % silica were tested to show their ability to convert propylene to an olefinic product. To test the catalyst formulations for catalytic performance, the catalysts were pressed into tablets and the tablets were broken into pieces and sieved.
In the preparation of the first catalyst sample, ZSM-23 zeolite powder with a silica to alumina molar ratio (SAR) of 46, and ZSM-5 zeolite powder with a SAR of 80 were used in the ammonium form in the weight ratio 50:50. Prior to mixing the powders, the ZSM-5 zeolite powder was treated with phosphorus, resulting in a catalyst that has only one zeolite pre-treated with phosphorus. Phosphorus was deposited on a ZSM-5 zeolite powder with a silica-to-alumina ratio of 80 by means of impregnation with an acidic solution containing phosphoric acid to obtain a ZSM-5 treated zeolite powder containing 2.0 wt % P. The ZSM-5 powder was calcined at 550° C. Then, the powder mix was added to an aqueous solution and subsequently the slurry was milled. Next, kaolin clay and a silica sol were added and the resulting mixture was spray dried wherein the weight-based average particle size was between 70-90 μm. The spray dried catalysts were exposed to ion-exchange using an ammonium nitrate solution. Then, phosphorus was deposited on the catalyst by means of impregnation using acidic solutions containing phosphoric acid (H3PO4). The concentration of the solution was adjusted to impregnate 1.0 wt % of phosphorus on the catalyst. After impregnation the catalysts were dried at 140° C. and then calcined at 550° C. for 2 hours. The final formulated catalyst thus obtained is further referred to as catalyst 1.
Another formulated catalyst was prepared as described herein above for catalyst 1, with the exception that only ZSM-5 with a SAR of 80 was used and it was not treated with phosphorus prior to spray-drying. The concentration of the phosphorus impregnation solution was adjusted to impregnate 1.5 wt % of phosphorus on the catalyst formulation. The final formulated catalyst thus obtained is further referred to as catalyst 2.
The phosphorus loading on the final catalysts is given based on the weight percentage of the elemental phosphorus in any phosphor species, based on the total weight of the formulated catalyst.
Propylene was reacted over the catalysts which were tested to determine their selectivity towards olefins, mainly ethylene and higher olefins. For the catalytic testing, a sieve fraction of 60-80 mesh was used. The reaction was performed using a quartz reactor tube of 1.8 mm internal diameter. The molecular sieve samples were heated in nitrogen to the reaction temperature and a mixture consisting of 3 vol % propylene and, in some tests, 6 vol % methanol, balanced with N2 was passed over the catalyst at atmospheric pressure (1 bar).
The Gas Hourly Space Velocity (GHSV) is determined by the total gas flow over the zeolite weight per unit time (ml gas)/(g zeolite·hr). The gas hourly space velocity used in the experiments was 19,000 (ml gas)/(g zeolite·hr). The effluent from the reactor was analyzed by gas chromatography (GC) to determine the product composition. The composition was calculated on a weight basis of all hydrocarbons analyzed. The composition was defined by the division of the mass of specific product by the sum of the masses of all products. The effluent from the reactor obtained at several reactor temperatures was analyzed. The results are shown in Table 1.
Example 2 was carried out in a similar manner to example 1 except that catalyst used in the tests was the molecular sieve itself: ZSM23 SAR46 (sample 1) and ZSM22 SAR100 (sample 2). A sieve fraction of 60-80 mesh is used for testing. The composition of the effluent is displayed in Table 2.
As can be seen from these results, recycled propylene fed to an OTO reactor with an oxygenate co-feed (methanol) can be converted to ethylene, C4 compounds and others.
This shows that a propylene recycle can effectively be used to reduce the amount of propylene produced and shift production to one of the other products of this OTO conversion. Propylene fed to an olefin cracking unit (exemplified by the examples without methanol co-feed) has a low conversion, so it is not preferred to recycle propylene to an olefin cracking unit.
| Number | Date | Country | Kind |
|---|---|---|---|
| 11195827.8 | Dec 2011 | EP | regional |
