Aromatic hydrocarbon production process

FIELD: petrochemical processes.

SUBSTANCE: feedstock is brought into contact with catalyst based on Pentasil family zeolite in at least two zones differing from each other in conditions of conversion of aliphatic hydrocarbons into aromatic hydrocarbons, first in low-temperature conversion zone to covert more active feedstock components to produce aromatic hydrocarbons containing product followed by recovering C5+-hydrocarbons therefrom and, then, contacting the rest of hydrocarbons produced in low-temperature conversion zone with catalyst in high-temperature conversion zone, wherein less active component(s) is converted into aromatic hydrocarbons containing product followed by recovering C5+-hydrocarbons therefrom.

EFFECT: enabled production of aromatic hydrocarbons under optimal conditions from feedstock containing aliphatic C1-C4-hydrocarbons with no necessity of separating the latter.

4 cl, 1 dwg, 1 tbl

 

The invention relates to methods of producing aromatic hydrocarbons from aliphatic and may be used in the refining and petrochemical industry.

Broad fraction of light hydrocarbons consisting mainly of propane and butane, are a by-product of gas production and gas processing companies. Lower paraffins and olefins is also obtained as by-products in oil refineries. Their excess can be recovered aromatic hydrocarbons using catalysts based on crednerite of metallasiloxanes having a high activity, selectivity and stability in the reaction of formation of aromatic hydrocarbons from aliphatic.

Most of the known methods for obtaining aromatic hydrocarbons from light aliphatic commodity flow consists mainly of hydrocarbons With1-C4and the transformation of raw materials carried out without separation of components in a single reaction zone, in the same conditions, while the propane is converted to aromatic hydrocarbons with high yield at a higher temperature than butane or propylene, and for the conversion of ethane requires an even higher temperature. Therefore, the contact of the mixed feedstock with a catalyst carried out either at high temperatures, focusing on less AK is positive components of raw materials, thereby increasing the rate of coke formation and reducing the lifetime of the catalyst, or at a lower temperature, with a relatively low degree of conversion of propane and ethane, with high recycling neprevyshenie raw materials. In other ways carry out the conversion of the raw material components in separate zones at the optimum for each component conditions.

The known method (US patent No. 5171912, 1992, 1/00 C 07 C) production of gasoline With5+enriched with aromatic hydrocarbons and/or paraffins5-C6from hydrocarbon feedstock containing paraffins3-C4using catalysts based on crednerite molecular sieves, including the division of raw materials waxes3-C4in the fractionation column to receive the head of a ring-containing propane, and the middle ring containing butane, contact stream containing propane, with a catalyst in the conversion zone at a temperature 260-482°s With gauge pressure of 0.35 to 10.5 MPa, the weight of the feed rate of the raw material of 0.1-10 h-1for the conversion of propane in the mixture that contains2+alkanes, the distillation of this mixture and obtaining deethanizing thread, containing3+alkanes, the contact ring containing butane with a catalyst at a temperature 246-427°s With gauge pressure of 2.8-14 MPa, the weight of the feed speed si is rd 0.1 to 50 h -1for the conversion of n-butane to propane and gasoline5+almost without formation of lighter hydrocarbons With3the introduction deethanizing product conversion of propane and product conversion of butane in the column fractionation of raw materials and the selection of the stream containing propane stream containing butane, and gasoline C5+.

To implement the described method requires use of highly active and highly selective catalysts that allow the conversion of propane and butane in the gasoline under mild conditions, with virtually no methane and ethane. In addition, in the above method does not solve the problem of energy security adiabatic conversion of propane and butane in aromatic hydrocarbons with high output.

The known method (patent RU №2175959, 2001, C 07 C 1/00, prototype) processing of aliphatic hydrocarbons2-C12presented in two streams respectively include light and heavy components in aromatic hydrocarbons or high-octane gasoline by contact of the feedstock with a catalyst containing a group zeolite, at least two zones with different conditions of conversion to products containing aromatic hydrocarbons. The method includes heating the raw material, the contact light components of the feedstock with the catalyst in the high temperature reaction zone, feeding the eye products from the high temperature reaction zone in the low-temperature reaction zone, contact heavy components of the feedstock with the catalyst in the low temperature area of the endothermic reaction and separation of the resulting product stream of hydrocarbons5+and a gas stream containing aliphatic hydrocarbons2-C4, part of which can be used as recycling. The described method solves the problem of energy supply the endothermic reaction of aromatization of paraffins with decreasing recycling coolant: the conversion of the raw material components is carried out in separate zones in the preferred conditions for the formation of aromatic hydrocarbons, and heat flow of products from the high temperature reaction zone is used to maintain the endothermic process in the low-temperature reaction zone. In the processing of the propane-butane fraction in this way will require a preliminary division into propane (light components raw materials) and butane (heavy raw material components).

The proposed method for obtaining aromatic hydrocarbons from a feedstock containing aliphatic hydrocarbons, solves the problem of turning them into separate zones without prior separation of raw materials as follows: the hydrocarbon feedstocks contact the catalyst consistently in the low-and high-temperature zones of dehydrocyclization, in the which become different activity components or groups of components. The task of ensuring a high degree of conversion of raw materials decide, using as a coolant in the low temperature zone at least part of the low-level components, raw materials, and in the high temperature zone, at least part of the methane and ethane obtained in the transformation of materials in the low temperature zone.

The method of obtaining aromatic hydrocarbons from hydrocarbons containing aliphatic hydrocarbons, involves the conversion of raw materials when in contact with a catalyst containing a group zeolite, at least two zones with different conditions the conversion of aliphatic hydrocarbons to aromatic and isolating from the resulting hydrocarbon products5+containing aromatic hydrocarbons, and differs in that the raw material is sent to the low-temperature conversion zone more active or more active aliphatic hydrocarbons, obtained from the product emit a stream of hydrocarbons5+and the remaining hydrocarbons are sent to a high-temperature conversion zone less active or less active aliphatic hydrocarbons.

As hydrocarbons containing aliphatic hydrocarbons may be used hydrocarbon fractions With2-C4including containing components5+: propane-butane fraction, broad fraction of light uglevodorov is s, and registereda fraction2-C4. The preferred propane-butane fraction containing butane 60-80% m

Used in the proposed method, the catalysts active in dehydrocyclization lower olefins and paraffins and containing aluminosilicate group zeolite or metroselect similar structures and at least one metal having dehydrating activity, such as platinum, chromium, zinc, cadmium, molybdenum, gallium. The catalyst may also contain phosphorus, fluorine, oxides of rare earth elements and other components that increase its activity, selectivity or stability in the reaction of formation of hydrocarbons With5+from aliphatic hydrocarbons. Such catalysts are widely known in the art. In different zones can be used the same or different composition of the catalysts that provide high conversion of raw materials and the selectivity of the formation of aromatic hydrocarbons. Upon contact with the catalyst in the areas of conversion of aliphatic hydrocarbons feedstock into a mixture of hydrocarbons, C1-C10containing mainly saturated gases With1-C4and aromatic hydrocarbons, mainly With6-C8.

Raw material components show different activity in the reaction of formation of aromatic hydrocarbons. Two is komponentov more active forms of aromatic hydrocarbons at a lower temperature. The more active alkanes and alkenes have higher molecular weight and with the same number of carbon atoms in the molecule the more olefins paraffins.

The contact of the feedstock with the catalyst is carried out in at least two reaction zones, characterized by the conversion of aliphatic hydrocarbons to aromatic, including average temperature in the area and, possibly, pressure and contact time of the feedstock with the catalyst. The preferred temperature for the conversion of propane - 530-600°, butane - 480-570°C, hydrocarbon, C5+- not above 550°C. Due to thermal effect of the chemical process of changing the temperature in the conversion zone is preferably not more than 30°C.

To obtain an aromatic hydrocarbon raw materials are not separated into fractions, but faction or individual hydrocarbons into separate zones sequentially: first, in areas with milder conditions of conversion is more active components and, possibly, some less active later in the area or in areas with more stringent conditions less active components. Hydrocarbons With5+almost in the same conditions to form aromatic hydrocarbons and mixed with them, so they form a single group of the most active components. Butane and propane are quite different activity, and preferably create two AOR is to convert them in optimal conditions. Upon receipt of the product with a high concentration of aromatic hydrocarbons, for example, from associated gas with low content of hydrocarbons, C5+last, it is advisable to process in one with the butane conversion zone more active components. Propane-propylene and butane-butylene fraction can be recovered aromatic hydrocarbons in two zones, and olefins in a low temperature. When the substrate temperature and other conditions in the areas of conversion are determined by the properties of the catalyst and in the preferred case, provide a high degree of conversion of the feedstock into aromatic hydrocarbons.

The raw material is heated and sent to the low-temperature conversion zone less active or less active components, in which the contact of the feedstock with a catalyst to obtain a product containing aromatic hydrocarbons, under conditions providing a high degree of conversion of these components, preferably not lower than 90%.

From the product obtained in the low-temperature conversion zone, known methods produce components5+including aromatic hydrocarbons. To do this, condense hydrocarbons5+when cooling or the cooling and compression of the product, then sephirot vapor-liquid mixture and stabilize the resulting hydrocarbon, C5+. P and this will also get the hydrocarbons 4-in the mixture formed in the chemical process by hydrogen comprising at least two vapor streams generated by separation and stabilization. Hydrocarbons With4-include methane, ethane, propane and butane raw materials and formed in the process of catalytic conversion. At least part of the selected hydrocarbons With4-containing less active in reactions of dehydrocyclization components, is heated and sent to a high-temperature zone.

In the high-temperature conversion zone shall contact of hydrocarbons With4-separated from the product of low-temperature zone conversion with the catalyst at a higher average temperature than in the low-temperature zone to obtain a product containing aromatic hydrocarbons. The inlet temperature in the high temperature zone of at least 20°With higher than at the entrance to the previous area.

The product obtained in the high temperature zone conversion, in addition to hydrocarbons, C5+includes neprevyshenie raw materials, methane, ethane and hydrogen. This product hydrocarbons With5+produce by known methods. Neprevyshenie in the first high temperature zone of the raw material components in the mixture with the products of C1-C4this zone can be allocated to the second high temperature zone. To achieve a more complete conversion of the less assets the components of raw materials can be arranged with their recycling in the last conversion zone. In addition, can be implemented recycling the hydrogen-containing gas used as a coolant in one or more zones of the conversion.

Stable products5+preferably get when stabilization of the mixture components, condensed by cooling and compression products to all areas of the conversion. From the obtained concentrate of aromatic hydrocarbons the individual components can be isolated by conventional methods.

Described is a method of obtaining aromatic hydrocarbons can be carried out as follows.

Example 1.

Raw material for obtaining a concentrate of aromatic hydrocarbon is propane-butane fraction (PBF)containing 0.8 wt.% Ethan, of 14.0 wt.% propane, 1.5 wt.% ISO-butane and 80.6 wt.% n-butane and 3.1 wt.% pentane. The catalyst prepared according to patent RU No. 2165293 and has the following composition in wt.%: the group zeolite (SiO2/Al2O3=60, the content of sodium oxide is less than 0.1 wt.%) - 62; zinc oxide - 1,8; the cerium oxide is 0.3; the oxide of lanthanum - 1,5; magnesium oxide is 0.2; aluminium oxide - 34,2. Low-temperature zone, the conversion of butane and pentane forms a layer of catalyst in the reactor, in which warm, partially providing the transformation of raw materials into specified conditions. High-temperature zone of the conversion of propane creates a layer of catalyst in an adiabatic reactor, is reversine propane to perform due to the heat content of the raw materials.

The block diagram of the process shown in the drawing. Characteristics of the main flow shown in the table with names reflecting their position in the block diagram of the process.

Raw propane-butane fraction LPG is mixed with recycle stream 12 and the obtained raw material 1 is directed in the reactor block I, where raw materials are heated in the recuperator heat exchangers and furnace to 550°and served in the reactor low temperature conversion of butane, which is in the process of catalytic conversion of raw materials at 550-520°and a pressure of about 0.8 MPa, the conversion of butane is 95%and the yield of the concentrate of aromatic hydrocarbons is 38.4 per cent. Product 2 low-temperature zone conversion enters the cooling unit and separation II, where it is cooled in air and water coolers to 25°and condensed hydrocarbons isolated in the low pressure separator. Vapour phase 3 of the low pressure separator unit cooling and separation II is mixed with a part of the vapor stream 8 from the high pressure separator unit cooling and separation of V and sent to the block compression and separation III, where komprimiert to 2.1 MPa, cooled to 25°and the resulting vapor-liquid mixture is separated in the high pressure separator. Vapor stream 5 hydrocarbons4-from the high pressure separator block compression and separation III contents the t with 23.3 wt.% propane and butane at a ratio of about 9:1 and is the raw material of the reactor block IV. In the reactor unit IV raw materials are heated in the recuperator heat exchangers and furnace to 575°and sent to the reactor high-temperature conversion of propane. High-temperature conversion of propane is carried out at a temperature 575-550°C and a pressure of about 2.0 MPa with selectivity 52,4% hydrocarbon, C5+(the concentrate of aromatic hydrocarbons). Product 7 of the high-temperature zone of the conversion of propane supplied to the cooling unit and separation of V, where it is cooled in air and water coolers to 25°and condensed components and vapor product stream is isolated in the high pressure separator. Resulting from the cooling unit and separation V vapor flow products high temperature zone conversion allocate recycled in this zone, the hydrocarbons4-and suvcw 9 from the high pressure separator is used as fuel gas. Liquid-phase stream 4 from the low pressure separator unit cooling and separation II, liquid-phase stream 6 from the high pressure separator block compression and separation III and liquid-phase stream 10 from the high pressure separator unit cooling and separation V mix obtained unstable liquid product of the process 11 and is directed to the stabilization unit VI, where in the recuperator heat exchanger is heated to 150°and sent to stabilization the column. The concentrate of aromatic hydrocarbons 13 (benzene content of 14.1%, toluene 45,3%, xylenes 23,0%, aromatic With9+10,7%) obtained when the cooling of the cubic product stabilizer in the recuperator heat exchanger of the stabilization unit (not shown). Gases stabilization 12 direct mixing with raw propane-butane fraction.

1. The method of obtaining aromatic hydrocarbons from hydrocarbons containing aliphatic hydrocarbons, which involves the conversion of raw materials when in contact with a catalyst containing a group zeolite, at least two zones with different conditions the conversion of aliphatic hydrocarbons to aromatic and isolating from the resulting hydrocarbon products5+containing aromatic hydrocarbons, characterized in that the raw materials are sent into the low-temperature conversion zone more active or more active aliphatic hydrocarbons, obtained from the product emit a stream of hydrocarbon, C5+and the remaining hydrocarbon product of low-temperature zone is sent to a high-temperature conversion zone less active or less active aliphatic hydrocarbons.

2. The method according to claim 1, wherein the hydrocarbon feedstock contains propane and butane.

3. The method according to claim 1, ex is different, however, what hydrocarbon feedstock contains components C5+butane and propane, and the contact of the feedstock with the catalyst is carried out in three areas: in the low-temperature conversion zone components5+in the high temperature zone of the conversion of butane in the high temperature zone of the conversion of propane.

4. The method according to any one of claims 1 to 3, characterized in that the separation of hydrocarbons From5+carried out at stabilization of the mixture components, condensed during compression and/or cooling of the products of each of the zones of the conversion.



 

Same patents:

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: invention relates to catalysts for isomerization of paraffins and alkylation of unsaturated and aromatic hydrocarbons contained in hydrocarbon stock. Catalyst of invention is characterized by that it lowers content of benzene and unsaturated hydrocarbons in gasoline fractions in above isomerization and alkylation process executed in presence of methanol and catalyst based on high-silica ZSM-5-type zeolite containing: 60.0-80.0% of iron-alumino-silicate with ZSM-5-type structure and silica ratio SiO2/Al2O3 = 20-160 and ratio SiO2/Fe2O3 = 30-550; 0.1-10.0% of modifying component selected from at least one of following metal oxides: copper, zinc, nickel, gallium, lanthanum, cerium, and rhenium; 0.5-5.0% of reinforcing additive: boron oxide, phosphorus oxide, or mixture thereof; the rest being alumina. Preparation of catalyst includes following steps: hydrothermal crystallization of reaction mixture at 120-180°C during 1 to 6 days, said reaction mixture being composed of precursors of silica, alumina, iron oxide, alkali metal oxide, hexamethylenediamine, and water; conversion of thus obtained iron-alumino-silicate into H-iron-alumino-silicate; further impregnation of iron-alumino-silicate with modifying metal compound followed by drying operation for 2 to 12 h at 110°C; mixing of dried material with reinforcing additive, with binder; mechanochemical treatment on vibrating mill for 4 to 72 h; molding catalyst paste; drying it for 0.1 to 24 h at 100-110°C; and calcination at 550-600°C for 0.1 to 24 h. Lowering of content of benzene and unsaturated hydrocarbons in gasoline fractions in presence of above catalyst is achieved during isomerization and alkylation of hydrocarbon feedstock carried out at 300-500°C, volumetric feedstock supply rate 2-4 h-1, weight ratio of hydrocarbon feedstock to methanol 1:(0.1-0.3), and pressure 0.1 to 1.5 MPa. In particular, hydrocarbon feedstock utilized is fraction 35-230°C of hydrostabilized liquid products of pyrolysis.

EFFECT: facilitated reduction of benzene and unsaturated hydrocarbons in gasoline fractions and other hydrocarbon fuel mixtures.

3 cl, 1 tbl, 13 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: hydrocarbon feed is converted in presence of porous catalyst at 250-500°C and pressure not higher than 2.5 MPa, feed uptake being not higher than 10 h-1. Hydrocarbon feed utilized are various-origin hydrocarbon distillates with dry point not higher than 400°C. Catalyst is selected from various aluminosilicate-type zeolites, gallosilicates, galloaluminosilicate, ferrosilicates, ferroaluminosilicates, chromosilicates, and chromoaluminosilicates with different elements incorporated into structure in synthesis stage. Resulting C1-C5-hydrocarbons are separated from gasoline and diesel fuel in separator and passed to second reactor filled with porous catalyst, wherein C1-C5-hydrocarbons are converted into concentrate of aromatic hydrocarbons with summary content of aromatics at least 95 wt %. In other embodiments of invention, products leaving second reactor are separated into gas and high-octane fraction. The latter is combined with straight-run gasoline fraction distilled from initial hydrocarbon feedstock.

EFFECT: increased average production of liquid products.

18 cl, 3 dwg, 9 ex

FIELD: petrochemical processes.

SUBSTANCE: high-octane fuels and propane-butane fraction are obtained via conversion of hydrocarbon feedstock on contact with hot catalyst placed in reactor, into which diluting gas is supplied at elevated pressure. Catalyst is Pentasil-type zeolite with general formula xM2/nO,xAl2O3,ySiO2,zMe2/mO wherein M represents hydrogen and/or metal cation, Me group II or VII metal, n is M cation valence, m is Me metal valence, x, y, z are numbers of moles of Al2O3, SiO2, and Me2/mO, respectively, and y/x and y/z ratios lie within a range of 5 to 1000. Metal oxide Me2/mO is formed during calcination, in presence of oxygen, of Me-containing insoluble compound obtained in zeolite reaction mixture.

EFFECT: increased octane number of gasoline fractions with propane-butane fraction as chief component of gas products, and prolonged inter-regeneration time of catalyst.

11 cl, 4 dwg, 3 tbl, 16 ex

The invention relates to the technology of organic synthesis, namely, catalytic methods of processing of hydrocarbon raw materials to produce products, which can be used either directly as motor fuel or as a component of a fuel or as raw material for separation of aromatic hydrocarbons and a catalyst for the implementation of these methods

The invention relates to the refining and petrochemical industries, in particular to methods of producing catalysts for the conversion of aliphatic hydrocarbons2-C12in high-octane gasoline and/or aromatic hydrocarbons

The invention relates to the production of motor fuels to the one-step catalytic process for the production of high-octane gasoline and diesel fuels with low sulfur content of various hydrocarbon materials with a high content of chemically stable sulfur compounds

The invention relates to the refining and petrochemical industries, in particular to methods of producing catalysts for the conversion of aliphatic hydrocarbons WITH2-C12in high-octane gasoline and/or aromatic hydrocarbons

The invention relates to the refining and petrochemical industries and is dedicated to the creation of the catalysts used in the processing of aliphatic hydrocarbons in the concentrate of aromatic hydrocarbons or high-octane component of gasoline

The invention relates to a technology for environmentally friendly high-octane gasoline and can be used in the refining and petrochemical industry to improve low-octane hydrocarbons in the presence of contact of the composition consisting of zeolite catalysts

FIELD: petroleum chemistry, chemical technology.

SUBSTANCE: hydrocarbons with high octane number are prepared from mixtures consisting of n-butane and isobutene, such as butanes from gaseous deposits. Method involves section for skeletal isomerization, section for dehydrogenation of paraffins, section for selective hydrogenation of butadiene and two sections for conversion of olefins. In these sections isobutene is converted selectively firstly by dimerization and/or esterification and then linear butenes are converted by alkylation. Then products from these two sections are combined to obtain product possessing with excellent properties for automobile engine (octane number, volatility and distillation curve).

EFFECT: improved preparing method of hydrocarbons.

8 cl, 1 dwg, 2 tbl, 1 ex

FIELD: organic chemistry, petroleum chemistry, chemical technology.

SUBSTANCE: method involves feeding isobutene-isobutylene-containing fraction to the combined synthesis of methyl-tert.-butyl ester and isobutylene dimmers by interaction with methanol at temperature 40-100 C in the presence of sulfocation-exchange resin as a catalyst. The combined esterification and oligomerization reaction is carried out in the mole ratio methanol : isobutylene = from 0.05-1.0 to 0.5-1.0 and volume rate of feeding reagents 2 h-1, not less. Also, method involves separation of the prepared reaction mixture for methyl-tert.-butyl ester, fraction of isobutylene dimmers and depleted isobutene fraction. Fraction of dimmers is separated at stage of distinct distillation off or rectification under reduced pressure 0.007-0.02 MPa. Invention provides increase yield of the end products, i. e. methyl-tert.-butyl ester and isobutylene dimmers.

EFFECT: improved preparing method.

FIELD: petrochemical industry; methods of hydrocarbon mixtures refining.

SUBSTANCE: the invention is pertaining to the field of petrochemical industry, in particular, to refining of the hydrocarbon mixtures. The invention provides for refining of a hydrocarbon mixture containing iso- and normal butanes and, probably, the butanes containing as a minimum two stages of the contacting with the solid high-acidic catalyst(s). The mixture first is exposed to refining at the stage(-s) mainly of the primary transformation of isobutene: from the product(-s) distil off a mixture of the non-reacted hydrocarbons C4, which then is exposed to a liquid-phase refining at the stage(-s) of the primary transformation of n-butanes and from the product distil off the non-reacted hydrocarbons containing predominary butanes. At the stage(-s) of the primary transformation of isobutene the contacting is carried out at the presence of water and-or alcoholC1-C2 in a quantity sufficient for transformation of the majority of isobytene into tret-butanol and-or into alkyl-tret-butyl ether. At the stage of primary transformation of n-butenes feed the mixture of the non-reacted hydrocarbons containing no more than 8 % of isobutene and admixture of water and-or alcohol from a previousa stage (-s) and the majority of n-butenes transform into dimers and codimers of n-butenes at the temperature of as a minimum by 15°C higher, than at the stage(-s) of the primary transformation of isobutene. The technical effect: transformation of the tret-alkenes into the oxygen-containing products having the high octane numbers.

EFFECT: the invention ensures transformation of the tret-alkenes into the oxygen-containing products having the high octane numbers.

11 cl, 2 tbl, 4 ex

FIELD: petrochemical processes.

SUBSTANCE: catalytic system, lower olefin, oligomerization medium are first provided. Reaction of lower olefin proceeds in presence of chromium-containing catalytic system to form product stream comprising higher olefinic product and rest of catalytic system, which are dispersed in process medium. Product is treated with suppressing substance, which is aliphatic secondary amine, alcohol, or combination thereof.

EFFECT: reduced corrosion of process equipment.

41 cl, 4 ex

The invention relates to the field of chemistry, in particular to a method for producing poly-alpha-olefins that can be used as a waxy base components of lubricating oils

The invention relates to catalytic chemistry, in particular to catalysts based on Nickel to obtain dimers and oligomers of olefins

The invention relates to the field of petrochemicals, in particular the production of trimers and tetramers of propylene, which are widely used as raw material in the manufacture of additives to oils, plasticizers, flotation agents and other surfactants and synthetic oils

FIELD: petrochemical processes.

SUBSTANCE: catalytic system, lower olefin, oligomerization medium are first provided. Reaction of lower olefin proceeds in presence of chromium-containing catalytic system to form product stream comprising higher olefinic product and rest of catalytic system, which are dispersed in process medium. Product is treated with suppressing substance, which is aliphatic secondary amine, alcohol, or combination thereof.

EFFECT: reduced corrosion of process equipment.

41 cl, 4 ex

Up!