Reactor system and method for ethylene oxide production

FIELD: engines and pumps; chemistry.

SUBSTANCE: reactor system comprises reactor tube, which contains compressed layer of molded carrier material, which may include catalytic component. Molded carrier material, for instance, aluminium oxide, has geometric configuration of hollow cylinder. Catalyst contains silver. Hollow cylinder has ratio of rated length to rated external diameter from 0.5 to 2, and ratio of rated external diameter to rated internal diameter, which exceeds 2.7. Reactor system also has such combinations of reactor tube diameter and geometric parameters of molded catalyst carrier, which make it possible to produce compressed layer of catalyst in reaction system with high density of package with minimum pressure drop via compressed layer of catalyst.

EFFECT: higher efficiency.

21 cl, 7 dwg, 3 tbl, 7 ex

 

This invention relates to a reactor system. Another aspect of this invention relates to the use of reactor systems in the production of ethylene oxide.

Ethylene oxide is an important industrial chemical used as a feedstock for the receipt of such chemicals as ethylene glycol, ethers of ethylene glycol, alkanolamine and detergents. One method for the production of ethylene oxide is carried out by means catalyzed partial oxidation of ethylene with oxygen. In this way the flow of the feedstock containing ethylene and oxygen, is passed over the layer of catalyst contained in the reaction zone which is maintained under certain reaction conditions. In a typical case, the reactor oxidation of ethylene is in the form of multiple parallel elongated tubes which are filled with catalyst particles on the media for the formation of a compacted layer contained inside the tubes of the reactor. The media can be of any shape, such as, for example, spheres, balls, rings and tablets. One particularly desirable form of the carrier is a hollow cylinder.

One problem associated with the use of compacted layer of catalyst particles on the carrier in the form of a hollow cylinder in the zone of oxidation reaction of ethylene is the difficulty in establishing a suitable balance between the differential giving is to be placed, which occurs through the catalyst bed during the implementation ethylenoxide process, and the packing density of the catalyst layer. Catalyst efficiency generally improves with an increase in the packing density of the catalyst in the reaction tubes oxidation of ethylene; however, an undesirable increase in pressure drop through the reactor is in General accompanied by an increased packing density of the catalyst.

In the production of ethylene oxide by the partial oxidation of ethylene is desirable to use a reactor system with a thickened layer of the catalyst having a high packing density, but with minimized pressure drop through a compacted layer of catalyst.

Thus, the objective of this invention is to provide a reactor system suitable for use in catalytic partial oxidation of ethylene oxide, which has a compacted layer of catalyst with high packing density, but still provides a suitable low pressure drop during operation.

Other aspects, objectives and some of the advantages of this invention will become more apparent in light of the following disclosure.

In one aspect, the invention can be defined as a reactor system containing

an elongated tube having a tube length and diameter of the pipes and, which define the reaction zone; and within the reaction zone contains a compacted layer having a certain form of material media; thus molded material of the carrier has a geometric configuration of a hollow cylinder, a certain nominal length nominal outside diameter and nominal internal diameter such that the ratio of nominal length nominal outside diameter is in the range from 0.5 to 2, and additionally so that

when the tube diameter is less than 28 mm, the ratio of the nominal outside diameter to the nominal internal diameter greater than 2.3 and the ratio of tube diameter to the external diameter is in the range from 1.5 to 7, and

when the tube diameter is equal to at least 28 mm, the ratio of the nominal outside diameter to the nominal internal diameter exceeding 2.7 and the ratio of tube diameter to the external diameter is in the range from 2 to 10.

In another aspect, the invention can be defined as a reactor system containing

an elongated tube having a tube length and tube diameter, which define the reaction zone; and within the reaction zone contains a compacted layer having a certain form of material media; thus molded material of the carrier has a geometric configuration of a hollow cylinder, determine lannou nominal length, nominal outside diameter and nominal internal diameter so that

the ratio of nominal length nominal outside diameter is in the range from 0.5 to 2 and

the ratio of the nominal outside diameter to the nominal inner diameter provides a positive test result, as hereinafter defined, and additionally so that

the ratio of tube diameter to the nominal outside diameter is in the range from 1.5 to 7, when the tube diameter is less than 28 mm, and in the interval from 2 to 10, when the tube diameter is equal to at least 28 mm

In this description of "positive test result" is determined by the decrease of the ratio of the numerical values of pressure drop per unit length of the compacted layer and the numerical values of the packing density, with these numerical values are obtained by testing of the compacted layer in a turbulent flow of gaseous nitrogen at a pressure of 1,136 MPa (150 psig) in relation to the comparative ratio of the numerical values obtained in an identical manner, except that the geometric configuration of the hollow cylinder of the same material of the carrier is determined by the nominal outside diameter of 6 mm and a nominal inner diameter of 2.6 mm, when the diameter of the tube is less than 28 mm, and a nominal outer diameter equal to 8 mm, and the nominal in the morning diameter equal to 3.2 mm, when the tube diameter is equal to at least 28 mm, and optionally the ratio of nominal length nominal external diameter equal to 1.

In accordance with another aspect of the present invention a method of production of ethylene oxide includes the steps that carry out the introduction in the reactor system in accordance with this invention a feedstock containing ethylene and oxygen, and removing from the reactor system, the reaction product containing ethylene oxide and neproreagirovavshimi ethylene, if he is, where within the reaction zone is a catalytic system on the media, which includes the catalytic component on the carrier of the molded material carrier having a geometrical configuration of a hollow cylinder.

Additionally, the invention provides a method of use of ethylene oxide to obtain ethylene glycol, simple ether of ethylene glycol or 1,2-alkanolamine, including the conversion of ethylene oxide to ethylene glycol, a simple ether of ethylene glycol or 1,2-alkanolamine, in which the ethylene oxide is produced by way of the obtain of ethylene oxide in accordance with this invention.

Used in this description in the context of the geometric configuration of a hollow cylinder, the terms "inner diameter and the diameter of the hole" have the same meaning and are used in the data description interchangeable. As used in this description, the terms "media" and "basis" have the same meaning and are used herein interchangeably.

Figure 1 shows some aspects of a reactor system according to this invention, which contains a tube having a length, which is filled with compacted layer containing molded material of the carrier of the catalytic system;

figure 2 shows a molded material of the carrier of the catalytic system according to this invention, which has a geometric configuration of a hollow cylinder and physical dimensions that characterize the molded material media;

figure 3 is a schematic representation of the method of production of ethylene oxide, which includes some new aspects of the present invention;

figure 4 presents data on changes ("C(%)") pressure drop ("% PD") and the packing density of the tube (PUT;% PUT*" represent duplicated data)resulting from the use of different sizes (outer diameters) of the material media in the form of a hollow cylinder with different relations of length to diameter ("DL/Dr") in the reactor tube with a diameter of 39 mm on the application of the standard 8 mm material media in the form of a hollow cylinder;

figure 5 presents data on changes ("C(%)") pressure drop ("% PD") and the packing density of the Tr is the KJV ("PUT"; "% PUT*" represent duplicated data)resulting from the use of different sizes (outer diameters) of the material media in the form of a hollow cylinder with respect to the nominal length to diameter, equal to 1.0, and different hole diameters ("HOLE" is marked in mm) in the reactor tube with a diameter of 39 mm on the application of the standard 8 mm material media in the form of a hollow cylinder;

6 presents data on changes ("C(%)") pressure drop ("% PD") and the packing density of the tube (PUT;% PUT*" represent duplicated data)resulting from the use of different sizes (outer diameters) of the material media in the form of a hollow cylinder with different relations of length to diameter ("DL/Dr") in the reactor tube with a diameter of 21 mm on the application of the standard 6-mm material media in the form of a hollow cylinder;

7 depicts a cross-sectional view of the outer perimeters (a) a molded material of the carrier, which is a perfect cylinder, and (b) cross section of a molded material of the carrier, which is the deviation from an ideal cylinder.

One method for the production of ethylene oxide shall be implemented by catalyzed partial oxidation of ethylene with oxygen. The method described in General terms in Kirk-Othmer, Encyclopedia of Chemical Technology, Volume 9, pp.432-471, John Wiley, London/New York 1980. Common R the actor system oxidation of ethylene are suitable for use in the present invention, and they include many parallel elongated tubes having internal diameters in the range from 20 mm to 60 mm and a length in the range from 3 to 15 mm are Also possible larger tube for use in a reactor system for the oxidation of ethylene. Tubes are usually suitable for use in heat exchangers shell-and-tube type and are formed in the beam for placement in the casing of the heat exchanger. The tubes are sealed in any suitable catalyst for the oxidation of ethylene, which provides partial oxidation of ethylene with oxygen to ethylene oxide. Tube heat exchanger provides passing the medium of heat transfer to remove heat of reaction in the oxidation of ethylene to control the reaction temperature inside the tubes containing the catalyst for the oxidation of ethylene.

The flow of the feedstock containing ethylene and oxygen, is introduced into the tube reactor system in which the flow of the feedstock in contact with a catalyst for oxidation of ethylene, typically at a temperature in the range from 50°With up to 400°and typically at a pressure in the range from 0.15 MPa to 3 MPa.

The catalytic system used in a typical production methods of ethylene oxide described above represents the catalytic system on the media, which includes a base material or substrate, on which is deposited or in which impregnorium catalytic component and, if desirable, the promoter component of the catalyst or components.

Reactor system according to this invention can be used in the oxidation of ethylene to ethylene oxide and includes a combination of the reactor tube and the molded material of the carrier, which is preferably a catalytic system. The unique geometry of this combination provides various unexpected advantages of the method.

Component catalytic system of the reactor system according to this invention may include a molded material of the carrier, which is the basis of the catalytic component. Optional molded material of the carrier is also the basis of one or more components of the promoters of the catalyst or components of copromotion catalysts. The preferred catalytic component is a silver. As for the promoter component, it may include, for example, rare earth metals, magnesium, rhenium and alkali metals such as lithium, sodium, potassium, rubidium and cesium. Among them, preferred are rhenium and alkali metals, in particular, of higher alkali metals such as lithium, potassium, rubidium and cesium. Most preferred among the higher alkali metal is cesium. Or rhenium promoter can be used without presents promoter of alkaline metal is, or promoter of the alkali metal can be used without presents rhenium promoter, or rhenium promoter and the promoter of the alkali metal can both be present in the catalytic system. In addition to the above promoters in the catalyst system may contain rhenium copromoter. Such copromotor may include sulfur, molybdenum, tungsten and chromium. Connection promoter and copromotor can be applied to the material of the carrier in any suitable manner, for example by impregnation, and in any form.

The material of the carrier molded material of the carrier and catalyst system can be any commercially available heat-resistant and porous material, suitable for use as a material of the carrier for the silver catalyst and promoter components of the catalytic system. Materials media should be relatively inert under the reaction conditions prevailing in the oxidation of ethylene, and in the presence of applied chemical compounds. The material of the carrier may include carbon, silicon carbide, silicon carbide, silicon dioxide, aluminum oxide and mixtures on the basis of aluminum oxide and silicon dioxide. It is preferable α-aluminium oxide, as it has a highly uniform pore size. The material of the carrier has in typical is the case of specific surface area, equal to from 0.1 to 10 m2/g, preferably from 0.2 to 5 m2/g and more preferably from 0.3 to 3 m2/g (measured well-known method B. E. T., see Brunauer, Emmet and Teller in J. Am. Chem. Soc. 60 (1938) 309-316, which is described in this description by reference); in a typical case, the specific pore volume of 0.1 to 1.5 cm3/g, preferably from 0.2 to 1.0 cm3/g and most preferably from 0.3 to 0.8 cm3/g (measured by the well known method of adsorption of water, which is ASTM C20); in a typical case, an apparent porosity of from 20 to 120% by volume, preferably from 40 to 80% by volume (measured by the method of adsorption of water); in a typical case, the average pore diameter of from 0.3 to 15 μm, preferably from 1 to 10 μm; and in a typical case, the percentage of pores having a diameter of from 0.03 to 10 μm, equal to at least 50% by weight (measured by mercury intrusion to pressure 3,0·108PA using Micromeretics Autopore 9200 (contact angle 130°, mercury with a surface tension equal to 0,473 N/m, and the applied correction for mercury compression).

The silver component of the catalyst and promoter components of the catalytic system are deposited on the material of the carrier or impregnorium in the material of the carrier of the catalytic system by any standard method known in this field. The catalytic system must typically be to the concentrations of silver or metallic silver in the range of from 2 mass% to 30 mass percent or even higher, for example, up to 40 weight percent, or up to 50 mass%, and the mass percentage based on the total weight of the catalytic system, including the mass of material of the carrier, the weight of the catalytic component, i.e. metallic silver, and the weight of the component or components of the promoter. In some embodiments, the implementation preferably, the silver component of the catalytic system was present at a concentration in the range of from 4 weight percent to 22 weight percent and most preferably from 6 to 20 mass percent. In other cases, it is preferable that the silver component catalytic system was present at a concentration in the range of from more than 20 to less than 30 mass% and more preferably from 22 to 28 weight percent. The promoter or promoters may be present in the catalytic system at a concentration in the range from 0.003 mass% to 1.0 mass%, preferably 0.005 mass% to 0.5 mass%, and most preferably from 0.01 to 0.2 mass%.

Reactor system according to the present invention provides an improved balance of the packing density of the tube (PCI), the porosity of the layer and delay of the catalyst relative to the pressure drop through a compacted layer when used in the method of production this is lanoxine compared with conventional systems. An important aspect of this invention is the recognition that such an improvement can be obtained, for example, by changing the relationship of the nominal outside diameter to the nominal internal diameter of the geometric configuration of a hollow cylinder. This conclusion is indeed unexpected, since the catalysts based on material media in the form of a hollow cylinder used in the methods of production of ethylene oxide for many years, and great efforts were expended to improve the performance of such a catalyst. However, attempts to improve the efficiency of these catalysts by modifying the geometry of the configuration of a hollow cylinder, apparently, has not received attention.

In accordance with this invention improved balance, receive, for example, by changing, in the typical case - increase the ratio of the nominal outside diameter to the nominal internal diameter of the geometric configuration of a hollow cylinder, compared with the ratio for the conventional material media in the form of a hollow cylinder. Improved balance can be found through comparative testing, as described earlier in this document, with the use of the material media in the form of a hollow cylinder in comparison with the standard material media in the form of a hollow cylinder, and housego common used sizes. In this comparative test materials typically have the same density of material. Otherwise, the difference in densities of the material is adjusted so that changes in the packing density of the tubes reflect the changes in the delay of the catalyst and the porosity of the layer. A positive test result as defined above in this description, is indicative for improved balance. Examples of comparative testing are presented in examples I-IV below in the description.

Improved balance-density packaging tube (PCI) in relation to the pressure drop through the compacted layer can be manifested in a variety of external or qualitative characteristics, as will be evident from the following description.

Reactor system according to the present invention includes a compacted layer molded material of the carrier or catalyst system, having a packing density of the tube higher than found in conventional reactor systems. In many cases it is desirable to increase the packing density of the tube due to the resulting advantages in catalyst efficiency. In General, however, it is expected that for higher density packaging tube pressure drop through a compacted layer, when used, will increase in relation to the standard reactor the m systems. Reactor system according to this invention, on the other hand, unexpectedly provides a smaller incremental increase in pressure drop through a compacted layer contained inside the tube reactor of the reactor system than expected, and, in many cases reducing the pressure drop through a compacted layer compared to conventional systems without the corresponding loss of the packing density of the tube and in many cases with the increase in the packing density of the tube.

Preferably, the reactor system according to this invention consisted of a compacted layer, having a density of packing of the tube at least as high as found in conventional reactor systems, but is preferably greater than the packing density of the tubes observed in the conventional systems, which when used are pressure drops, which fall together with the above-mentioned increase in the packing density of the tube.

The relative geometrical parameters between the tubing and molded by the media and/or catalytic systems are an important feature of the reactor system according to this invention, which includes a combination of a reactor tube Packed with a layer of molded carriers, which preferably includes a catalytic components to provide a catalytic system is eat. Is also unexpected that the larger carriers relative to the reactor tube can be downloaded in the form of a compacted layer inside the reactor tube for receiving increasing the packing density of the tube or without supervision larger pressure drop through a compacted layer when the reactor system is used, or with the supervision of an incremental increase in pressure drop that is less than expected, especially based on some engineering correlations, such as correlation Argana, see W.J. Beek and K.M.K. Muttzall, "Transport Phenomena", J. Wiley and Sons Ltd, 1975, p.114.

Larger carriers and catalytic systems are particularly desirable for use in a compressed layer of the reactor system according to this invention with reinforced layer having a higher packing density of the tube than expected for the particular size of the carrier or catalyst system, but which provides no incremental lowering of the pressure drop when using and preferably an incremental decrease in differential pressure with respect to such who are waiting for reactor systems with the same packing density of the tube. An additional advantage may be the increase in the packing density of the tube.

To obtain the above advantages reactor system of the present invention should be particularly the e geometrical ratio. Also determined that these geometrical parameters are influenced by the diameter of the reactor tubes and, thus, the relative geometrical parameters of the reactor tube and molded carriers are usually different for different tube diameters. For the reactor tubes having an inner diameter of less than 28 mm, the ratio of the inner diameter of the reactor tube and the outer diameter of the system carrier should be in the range from 1.5 to 7, preferably from 2 to 6 and most preferably from 2.5 to 5. For the reactor tubes having an inner diameter greater than 28 mm, the ratio of the inner diameter of the reactor tube and the external diameter of the catalyst carrier should be in the range from 2 to 10, preferably from 2.5 to 7.5 and most preferably from 3 to 5.

The ratio of the outer diameter to the inner diameter or the diameter of the hole of the carrier of the catalytic system is another important characteristic of the reactor system according to this invention. For the reactor tubes having an inner diameter of less than 28 mm, the ratio of the outer diameter to the bore diameter or the inner diameter of the carrier of the catalytic system may be in the range from 2.3 to 1000, preferably from 2.6 to 500 and most preferably from 2.9 to 200. For the reactor tubes having an inner diameter, excellent is superior to 28 mm, the ratio of the outer diameter to the bore diameter or the inner diameter of the carrier of the catalytic system may be in the range from 2.7 to 1000, preferably from 3 to 500 and most preferably from 3.3 to 250.

At that time, as it is important that the diameter of the hole of the molded material of the carrier was relatively small, it is also important that the inner hole of the carrier had at least a certain size. It was found that the pore volume determined by the diameter of the hole, provides some advantages in the production of the catalyst and its catalytic properties. Not limited to any particular theory, I believe, however, that the pore volume provided by the bore diameter of the hollow cylinder allows for improved deposition of the catalytic component on a carrier, for example by the application, and improved additional manipulation, such as drying. The advantage of using a relatively small diameter holes is that the molded material of the carrier has a large crushing strength compared to the material of the carrier having the larger diameter holes. It is preferable to have at least one end of the hole, in the typical case - on both ends - hole diameter equal to at least 0.1 mm, more predpochtitel is about, at least 0,2 mm, Preferably a diameter of the hole is equal to at least 5 mm and preferably up to 2 mm, for example 1 mm or 1.5 mm

An additional important characteristic of the reactor system according to this invention is that the carrier of the catalytic system of the compacted layer of the reactor system according to this invention has a ratio of length to external diameter in the range from 0.5 to 2.0, preferably from 0.8 to 1.5, and most preferably from 0.9 to 1.1.

Summary data desired intervals for the geometric dimensions of the reactor system according to this invention are presented in tables 1 and 2. Table 1 represents the relative geometrical parameters molded carriers for the reactor tubes having diameters of less than 28 mm table 2 represents the relative geometrical parameters molded carriers for the reactor tubes having diameters equal to at least 28 mm Smaller reactor tube may have a diameter tubes, which are in the range down to 21 mm or even less, for example 20 mm, Thus, the diameter of the smaller tube of the reactor tubes of the reactor system according to the present invention can be in the range from 20 mm or 21 mm to less than 28 mm larger reactor tube may have a diameter tubes that are in the interval up to 60 the m or even larger. Thus, the diameter of the larger tube of the reactor tubes of the reactor system according to the present invention can be in the range from 28 mm to 60 mm

For tube diameters in the range from 28 mm to 60 mm, in particular, when the tube diameter is 39 mm, the ratio of the nominal outside diameter to the nominal inner diameter of the carrier is preferably equal to:

at least, 4,5, when the outer diameter is in the range between 10.4 mm to 11.6 mm; or

more 3,4, specifically, at least 3,6, when the outer diameter is in the range from 9.4 mm to 10.6 mm; or

at least 2.6, specifically, in the range from 2.6 to 7.3, when the outer diameter is in the range from 8.4 mm to 9.6 mm

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Table 1

The geometrical parameters of the reactor system according to this invention for the reactor tubes having tube diameters less than 28 mm
Tube diameter/outer diameter of the catalytic systemThe length of the catalytic system/outer diameter catalytic systemThe external diameter of the catalyst/hole diameter
Wide1,5-70,5-22,3-1000
Intermediate2-60,8-1,52,6-500
2,5-50,9-1,12,9-200
Table 2

The geometrical parameters of the reactor system according to this invention for the reactor tubes having tube diameters equal to at least 28 mm
Tube diameter/outer diameter of the catalytic systemThe length of the catalytic system/outer diameter catalytic systemThe external diameter of the catalyst/hole diameter
Wide2-100,5-22,7-1000
Intermediate2,5-7,50,8-1,53,0-500
Narrow3-50,9-1,13,3-250

The reactor tube may be of any length, which effectively provides the necessary contact time in the reaction zone between the source reagents catalytic system to obtain the desired reaction product. In General, as noted above, the length of the reactor tube will exceed 3 m, and preferably it is in the range from 3 m to 15 m total length of the reactor tube can be Packed catalytic system, or any portion of the reactor tube can be Packed catalytic system for providing, thus, sealed with the HHS catalytic system, with the depth of the layer. Thus, the depth of the layer may exceed 3 m, and preferably it ranges from 3 meters to 15 meters.

In the normal practice of this invention the main part of the consolidated layer of the reactor system according to this invention includes a molded material of the carrier, with geometrical parameters, as described in this description. Thus, in a typical case, a compacted layer of the reactor system will be the predominant way that is at least 50 percent, to contain the catalytic system, which is specifically defined geometrical parameters, and specifically at least 80 percent of the compacted layer of the catalyst will contain certain specific catalytic system, but preferably at least 85% and most preferably 90 percent. When referring to the percentage of the compacted layer, which contains the catalytic system, this would mean the ratio of total number of individual particles of a catalytic system having specific dimensions described here, the total number of particles of the catalyst system contained in a compact layer, multiplied by 100. In yet another embodiment, when referring to the percentage of the compacted layer, which contains the catalytic system, this will mean agains the bulk volume of the particles of the catalytic system, having specific dimensions described here, to the bulk volume of all particles of a catalytic system contained in a compact layer, multiplied by 100. In yet another embodiment, when referring to the percentage of the compacted layer, which contains the catalytic system, this would mean the ratio of the mass of the particles of the catalytic system, with specific dimensions described here, to the mass of all particles of the catalyst system contained in a compact layer, multiplied by 100.

The packing density of the tube layer of a catalytic system of the reactor system according to this invention can be an important feature of the present invention, since improving the efficiency of the catalyst can be a result of an increase in the packing density of the tube obtained from the use of the unique geometries of the reactor system according to this invention. In General, the packing density of the tube compacted layer of a catalytic system depends on the inner diameter of the associated reactor tube and from properties, such as density, specific material media that is used for the formation of a molded product.

For the smaller internal diameter of the reactor tube packing density tube compacted layer may in General be less than the density of the packing tube compacted layer of larger internal diameter of the reactor tube. Thus, for example, the packing density of the tube compacted layer of the reactor system according to this invention, having an inner diameter of the reactor tube, equal to 21 mm, can be so low, but with excess as 550 kg per cubic meter, when the material of the carrier is mainly αaluminum oxide. For a reactor tube having a larger inner diameter of the tube, and tubes having a smaller diameter, it is desirable to have such a high packing density of the tube, as far as attainable, and still realize the benefits of the invention. This packing density of the tube, when the material of the carrier is mainly αaluminum oxide, may exceed 650 kg per cubic meter or be higher than 700 kg per cubic meter or even above 850 kg per cubic meter. Preferably the packing density of the tube exceeds 900 kg per cubic meter and most preferably the packing density of the tube greater than 920 kg per cubic meter. The packing density of the tube in the General case will be less than 1200 kg per cubic meter and, more specifically, less than 1150 kg per cubic meter.

1 shows a reactor system 10 according to this invention, containing an elongated tube 12 and a compacted layer 14 located in the elongated tube 12. Elongated tube 12 has a tube wall 16 with the inner surface is part of tube 18, which contains a compacted layer 14, and the diameter of the reaction zone 20. Elongated tube 12 has a length of tube 22 and a compacted layer 14 contained in the reaction zone has a depth of 24. Out of the depth of the layer 24 of the elongated tube 12 may include a separate layer of particles of a non-catalytic material, for example, heat exchange with the raw material and/or another separate layer, for example, heat exchange with the reaction product. Elongated tube 12 additionally has an input end of the tube 26, which may be injected feedstock containing ethylene and oxygen, and the output end of the tube 28, which may leave the reaction product containing ethylene oxide and ethylene. Note that the ethylene in the reaction product, if it contains, represents ethylene feedstock, which passes through the reactor unconverted. Typical values for the conversion of ethylene is greater than 10 molar percent, but in some cases, conversion may be less.

A compacted layer 14 contained in the reaction zone, consists of a layer of the catalytic system on the carrier 30, as shown in figure 2. The catalytic system on the carrier 30 is in the General case, the geometric configuration of a hollow cylinder with a nominal length 32, nominal outer diameter 34 and a nominal inner diameter or the diameter of the hole 36 in accordance with the laws the AI with this invention.

To a person skilled in the art it is obvious that the term "cylinder" does not necessarily mean that the geometrical configuration of the hollow cylinder includes an exact cylinder. Assume that the term "cylinder" includes minor deviations from the exact cylinder. For example, the transverse size of the outer perimeter of the geometric configuration of a hollow cylinder, perpendicular to the axis of the cylinder, is not necessarily accurate range 71, as shown in Fig.7. Also, the axis of the geometric configuration of the hollow cylinder may be approximately straight, and/or outer diameter of the geometric configuration of the hollow cylinder may be approximately constant along the axis. Minor variations include, for example, when the outer diameter of the cylinder can be located in an imaginary tubular space defined by two imaginary exact auxilii cylinders with virtual identical diameters, whereby the diameter of an imaginary inner cylinder is equal to at least 70%, more typically at least 80%, particularly at least 90% of the diameter of an imaginary outer cylinder, and imaginary cylinders are selected so that the ratio of their diameters is the most possible 1. In such instances, it is believed that the diameter of the imaginary vneshnej the cylinder is the outer diameter of the geometric configuration of a hollow cylinder. 7 shows a cross-section made perpendicular to the axis of the imaginary cylinder 73 and 74, the outer perimeter 72 of the geometric configuration of a hollow cylinder, an imaginary outer cylinder 73 and imaginary inner cylinder 74.

Similar to a person skilled in the art it is obvious that the hole geometric configuration of the hollow cylinder is not necessarily exactly cylindrical, the axis of the hole may be approximately straight, the hole diameter may be approximately constant, and/or the axis of the hole may be removed or be at an angle relative to the axis of the cylinder. If the hole diameter varies along the length of the holes, believe that the hole diameter is the largest diameter at the end of the hole. If the hole is not exactly circular in cross section, the wide size is the diameter of the hole. Also, the pore volume provided by the hole, can be divided into two or more apertures, such as 2, 3 or even 4 or 5 holes; in this case, the diameters of the holes are such that the total sum of the areas of cross sections of holes of equal cross-sectional area of a single hole having a diameter, as indicated in this specification.

In preferred embodiments, the implementation of the geometric configuration is oracea hollow cylinder is to be a cylinder having a hole along the axis of the cylinder.

It should be understood that the geometrical configuration of the hollow cylinder are nominal and approximate methods for manufacturing molded agglomerates are not necessarily exact.

It is a unique geometric combination of the internal tube diameter or diameter of the reaction zone 20 and the geometric dimensions of the catalytic system on the carrier 30 provides an unexpected reduction in pressure drop when it is used with respect to conventional systems, without significant reduction in the packing density of the tube. In many cases, and preferably the density of the packing tube reaction system according to this invention is greater than for conventional systems, still providing at the same time reducing the pressure drop when using.

Significant geometric size of the catalytic system 30 is the ratio of nominal length 32 to the nominal external diameter of 34. This size is described in detail above.

Another significant geometric size of the catalytic system 30 is the ratio of the nominal outside diameter 34 to the nominal inner diameter 36. This size is described in detail above.

The relative dimensions between the catalytic system 30 and lengthened the second tube 12 are an important aspect of this invention, because these dimensions determine the packing density of the tube and the characteristics of the pressure drop associated with the reactor system 10. This size is described in detail above.

Another way to determine the catalytic system is a reference to its nominal dimensions. For a standard 8-mm catalyst having a geometrical configuration of a hollow cylinder, the outer cylinder diameter nominally equal to 8 mm, but may be in the range of 7.4 mm to 8.6 mm Length cylinder nominally equal to 8 mm, but may be in the range of 7.4 mm to 8.6 mm For use in this invention the diameter of the hole may be equal to at least 0.1 mm or 0.2 mm, and preferably in the range from 0.5 mm to 3.5 mm, more preferably from 0.5 mm to less than 3 mm.

For a standard 9-mm catalyst having a geometrical configuration of a hollow cylinder, the outer cylinder diameter generally equal to 9 mm, but may be in the range from 8.4 mm to 9.6 mm, the length of the cylinder, while nominally equal to 9 mm, can be in the range from 8.4 mm to 9.6 mm For use in this invention the diameter of the hole standard 9-mm catalyst may be equal to at least 0.1 mm or 0.2 mm and preferably is in the range from 0.5 mm to 3.5 mm, more preferably from 1.25 mm to 3.5 mm

For a standard 10-mm catalyst having geo is eticheskuyu configuration of a hollow cylinder, the external diameter of the cylinder is usually equal to 10 mm, but may be in the range from 9.4 mm to 10.6 mm, the length of the cylinder, while nominally equal to 10 mm, may be in the range from 9.4 mm to 10.6 mm For use in this invention the diameter of the hole standard 10-mm catalyst may be equal to at least 0.1 mm or 0.2 mm and preferably is in the range from 0.5 mm to 4.0 mm, more preferably from 0.5 mm to 3 mm, even more preferably from 0.5 mm to 2.8 mm

For a standard 11-mm catalyst having a geometrical configuration of a hollow cylinder, the outer cylinder diameter generally equal to 11 mm, but may be in the range of 10.4 mm to 11.6 mm, the length of the cylinder, while nominally equal to 11 mm, can be in the range of 10.4 mm to 11.6 mm For use in this invention the diameter of the hole standard 11-mm catalyst may be equal to at least 0.1 mm or 0.2 mm and preferably is in the range from 0.5 mm to 3.5 mm, more preferably from 0.5 mm to 2.5 mm

Large variability in the size of the catalytic system due to the way in which media is in the form of a hollow cylinder. The methods of production are known in the production of catalytic media and include such standard methods as extrusion methods and ways PR is the production of pellets.

Figure 3 is a schematic view showing the General method of production of ethylene oxide 40 with shell-and-tube heat exchanger 42, which is equipped with multiple reactor systems, as shown in figure 1. In a typical case, the reactor system of figure 1 are grouped together with many other reactor systems in the beam tubes to enter into the casing shell-and-tube heat exchanger.

The feedstock containing ethylene and oxygen, load through line 44 to the side of the tube shell-and-tube heat exchanger 42 where it is in contact with a catalytic system that is contained in it. Heat of reaction is removed through the use of fluid heat transfer, such as oil, kerosene or water, which are loaded from the side of the casing shell-and-tube heat exchanger 42 through pipe 46, and teploperenosa fluid is removed from the casing shell-and-tube heat exchanger 42 through line 48.

The reaction product containing ethylene oxide, unreacted ethylene, unreacted oxygen and, optionally, other reaction products such as carbon dioxide and water, is shown from a tube reactor system shell-and-tube heat exchanger 42 through line 50 and is held in the separation system 52. The separation system 52 provides the separation of ethylene oxide and ethylene and, if present, carbon dioxide and water. The extraction fluid, such as water, can be used to separate these components and introduced into the separation system 52 through pipe 54. Enriched extraction fluid out of the separation system 52 through line 56, while the unreacted ethylene and carbon dioxide, if present, out of the separation system 52 through line 58. Separated carbon dioxide exits the separation system 52 through line 61. Part of the gas stream passing through the pipe 58 may be removed as a bleed stream through line 60. The remaining gas stream passes through line 62 for recirculation compressor 64. The flow of the feedstock containing ethylene and oxygen passes through the pipe 66 and is combined with the recycle ethylene, which passes through the pipe 62, and the combined stream passes to the recirculation compressor 64. The recirculation compressor 64 is discharged into the pipe 44, whereby paged stream is fed to the input side of the tube shell-and-tube heat exchanger 42. Mainly the separation system 52 operates so that the amount of carbon dioxide in the flow of the feedstock through line 44 is low, in the example below 2 mol %, preferably less than 1 mol % or in the range from 0.5 to 1 mol %.

Ethylene oxide, obtained in the method of epoxidation can be converted into ethylene, a simple ether of ethylene glycol or alkanolamine.

Conversion to ethylene glycol or a simple ester of ethylene glycol may include, for example, the interaction of ethylene oxide with water, appropriately using acidic or basic catalyst. For example, to obtain mainly of ethylene glycol and less simple ether of ethylene glycol, the ethylene oxide can interact with a tenfold molar excess of water in the liquid-phase reaction in the presence of an acid catalyst, for example of 0.5-1.0 wt.% sulfuric acid, in the calculation of the total reaction mixture at 50 to 70°With, at an absolute pressure of 100 kPa or in gas-phase reactions in 130-240°and an absolute pressure of 2000-4000 kPa, preferably in the absence of catalyst. If the composite fraction of water decreases, the aggregate share of ethers of ethylene glycol in the reaction mixture increases. Ethers of ethylene glycol, thus obtained, can be a fluids, triavir, tetraethyl or subsequent broadcast. Alternative ethers of ethylene glycol can be obtained through the conversion of ethylene oxide with an alcohol, especially a primary alcohol, such as meta is ol or ethanol, by replacing at least part of the water with alcohol.

Conversion to alkanolamine may include the interaction of ethylene oxide with an amine, such as ammonia, alkylamine or dialkylamino. Can be used in anhydrous or aqueous ammonia. Anhydrous ammonia is typically used to create favorable conditions for obtaining monoalkanolamines. For methods used in the conversion of ethylene oxide in alkanolamine may be, for example, the patent US-A-4845296, which is included in this description by reference.

Ethylene glycol and ethers of ethylene glycol have a wide variety of industrial applications, for example, in the industries of food, beverages, tobacco, cosmetics, thermoplastic polymers, thermosetting resin systems, detergents, heat transfer systems, etc. Alkanolamine can be used, for example, processing of natural gas ("the removal of acid gases and sulfur compounds").

The following examples are intended to illustrate the advantages of the present invention and are not intended for any limitation of the scope of the invention.

Example I

This example I represents the testing methodology used to assess the characteristics of the differential pressure and the packing density of the tube reactor system according to this invention in relation to standartjelektro system.

Various media in the form of a hollow cylinder, having different dimensions and geometric parameters tested in the reactor tube industrial length with an inner diameter or 39 mm or 21 mm Reactor tube set for measuring the difference of pressure drop through the layer of the device. Determine the packing density of the tube layer media.

Specific media for testing loaded into the reactor tube, applying a standard way of loading through the funnel. The carrier is weighed to determine its mass before it is loaded into the reactor tube. After loading the reactor tube carrier use the air source with a pressure of 0.79 MPa (100 psig for blowing dust for 15 seconds. Measure the height of the layer of the media.

The packing density of the tube determine, using the mass media loaded in the reactor tube, the measured height of the layer of the carrier and the inner diameter of the reactor tube. The packing density of the tube has units of mass per volume, and it is determined by the following formula:

4m/πd2h,

where m is the media loaded in the reactor tube,

d represents the diameter of the reactor tube and

h represents the height of the layer of the medium contained within the reactor tube.

After loading the reactor tube carrier of its seal and tester the Ute pressure 1,342 MPa (180 psig). The reactor tube is equipped with input and output. Gaseous nitrogen is injected into the Packed entrance of the reactor tube at a pressure of approximately 1,136 MPa (150 psig). For each of the approximately 11 different gas flow rates in the turbulent flow regime (number particle Reynolds more than 700, see W.J. Beek and K.M.K. Muttzall, "Transport Phenomena", J. Wiley and Sons Ltd, 1975, p.114) the difference of the differential pressure (pressure drop) through the layer of the device of the reactor tube is determined by measuring the inlet pressure tube and the output pressure tube. Also measure the temperature of the gaseous nitrogen at the inlet and outlet. The differential pressure value per unit length of the compacted layer. The packing density of the tube adjust for small differences in the characteristic densities of materials in various media to reflect differences in the delay of the catalyst caused by differences of the geometric parameters of the media.

Example II

This example II represents the sum of the results of applying the test described in example I for the media in the form of a hollow cylinder with a nominal size of 5 mm, 6 mm, 7 mm, 8 mm and 9 mm, with a nominal ratio of length to diameter (L/D) (hereinafter L/D)equal to either 0.5 or 1.0, Packed in a 39 mm of the reactor tube. The following data are the concrete results of the dimensions of the media:

9 mm: L/D=1,0, di is the m hole of 3.85 mm

9 mm: L/D=0.5, the diameter of the hole 3,90 mm

8 mm: L/D=1.0, the diameter of the hole 3,20 mm (standard 8 mm")

8 mm: L/D=0.5, the diameter of the hole 3,30 mm

7 mm: L/D=1.0, the diameter of the hole is 2.74 mm

7 mm: L/D=0.5, the hole diameter of 2.75 mm

6 mm: L/D=1.0, the diameter of the hole 2,60 mm (standard 6 mm")

6 mm: L/D=0.5, the diameter of the hole 2.60mm

5 mm: L/D=1.0, the diameter of the hole 2.40 mm

5 mm: L/D=0.5, the diameter of the hole 2,70 mm

Summary data for the percentage change of the pressure drop through the layer of the medium and the percentage change in the packing density of the tube in relation to the standard 8-mm media presented on figure 4. As shown, the dimensions of the media less than 8 mm and for all sizes of media, with the ratio L/D of 0.5, the pressure drop through the layer of the device increases. The data presented in figure 4 show, however, that a 39-mm reactor tube, a larger 9 mm media that has a ratio L/D equal to 1.0, provides improved pressure drop in relation to the standard 8-mm media.

Example III

This example III presents the results of applying the test described in example I for the cylindrical media with a nominal size of 9 mm, 10 mm, 11 mm, with a nominal ratio of length to diameter L/D equal to 1.0 in 39 mm of the reactor tube. Some of these carriers are solid cylinders, the other is the whether are hollow cylinders with different pore diameters, as indicated in figure 5. Summary data for the percentage change of the pressure drop through the layer of the medium and the percentage change in the packing density of the tube in relation to the standard 8-mm media presented on figure 5.

The data presented in figure 5, show an unexpected decrease in pressure drop, which is the result of applying a unique combination of the reactor tube and the geometry of the media. For 9-mm media, with the ratio of hole diameter to the external diameter greater was 0.138 (the ratio of the outer diameter to the diameter of the hole is less than 7,2), there is improvement in pressure drop relative to the standard test 8 mm carrier, and for all tested 10-mm and 11-mm media there is an improvement in pressure drop relative to the standard 8-mm media.

As for the densities of the packaging tube, the improvement observed for the densities of the packing tube with 9-mm carrier in relation to the standard 8-mm media for geometries in which the ratio of hole diameter to the external diameter equal to or greater than approximately 0,38 (the ratio of the outer diameter to the diameter of the hole, at least equal to 2.6), and for 10-mm media improvement observed for geometries with respect to the hole diameter to the external diameter equal to or less than approximately 0,28 (the ratio of the outer diameter to the yameru more holes 3,4, preferably, at least a 3.6). For 11-mm media improve observe as for differential pressure and density packaging tubes for all tested geometries that occurs when the ratio of the outer diameter to the diameter of the hole more than 4.5.

Example IV

This example IV presents the results of applying the test described in example I for the nominal media sizes 5 mm, 6 mm, 7 mm, 8 mm and 9 mm, with a nominal ratio L/D, or equal to 0.5, or 1, packaged in a 21-mm reactor tube. Specific data on the dimensions of the media outlined in example II.

Summary data for the percentage change of the pressure drop through the layer of the medium and the percentage change in the packing density of the tube in relation to the standard 6-mm media presented on Fig.6. As shown, for media sizes 8 mm and 9 mm see improvement in pressure drop, and 7-mm media with L/D equal to 1.0, see improvement in pressure drop. With the selected media can be achieved by improving the differential pressure without reducing the packing density of the tube, especially when the increase of the ratio of external diameter to the diameter of the hole.

Example V a (hypothetical)

Each of the carriers described in examples II-IV, impregnorium solution containing silver to form a silver catalyst containing Eitel. The flow of the feedstock containing ethylene and oxygen, further contact with the catalyst under suitable conditions for the formation of ethylene oxide.

Example VI

This example VI provides information regarding the properties and geometric configuration of the two types of media (e.g., the media and the media D)used in obtaining catalysts as described in example VII (see table 3).

Table 3

The properties of the media
MediaMedia D
Properties
Water absorption, %46,550,4
Volumetric packing density, kg/m3(lb/ft3)843 (52,7)788 (49,2)
Loss during abrasion ASTM, %14,716,5
The average force of destruction on a flat plate, N (lb)130 (29,3)180 (40,4)
Surface area, m2/g0,770,78
Geometrical configuration
Nominal size mm88
The average length, mm7,7
Length, intervalof 6.6 and 8.6of 6.6 and 8.6
Diameter, mm8,68,6
The hole diameter, mm1,021,02
Ratio length/outer diameter0,900,90

Example VII

In example VII describes the obtaining of catalysts that can be used in the present invention.

The catalyst With:

The catalyst is produced by application of media, using methods known from US-A-4766105, whereby this U.S. patent is given in this specification as a reference. The final composition of the catalyst is: 17,8% Ag, 460 ppm Cs/g of catalyst, 1.5 mmol Re/g of catalyst, 0.75 µmol W/g of catalyst and 15 mmol Li/g of catalyst.

The catalyst D:

Catalyst D get in the two-step impregnation. When the first application media impregnorium solution of silver in accordance with the procedure for catalyst C, except that the solution of silver do not add additives. After drying the resulting dried catalyst precursor contains about 17 wt.% silver. The dried catalyst precursor further impregnorium solution that contains silver and additives. The final composition of catalyst D with what is: 27,3% Ag, 550 ppm Cs/g of catalyst, 2.4 µmol Re/g of catalyst, of 0.60 µmol W/g of catalyst and 12 mmol Li/g of catalyst.

Catalyst E:

Catalyst E get in the two-step impregnation in accordance with the methodology used for catalyst D, except that the compound of tungsten is present in the first solution instead of the second impregnation solution for impregnation. The final composition of catalyst E is: 27,3% Ag, 560 ppm Cs/g of catalyst, 2.4 µmol Re/g of catalyst, of 0.60 µmol W/g of catalyst and 12 mmol Li/g of catalyst.

While the invention is described from the point of view presents a preferred variant of the invention, a reasonable variation and modification are possible for specialists in this field. Such variations and modifications are within the scope of the described invention and the appended claims.

1. Reactor system containing

an elongated tube having a reaction zone formed by the length and diameter of the tube, and the tube diameter is equal to at least 28 mm; and within the reaction zone contains a compacted layer of molded material carrier having a geometrical configuration of a hollow cylinder, a certain nominal length nominal outside diameter and nominal internal diameter thus the om, what is the ratio of nominal length nominal outside diameter is in the range from 0.5 to 2, and additionally so that

the ratio of the nominal outside diameter to the nominal internal diameter exceeding 2.7 and the ratio of tube diameter to the external diameter is in the range from 2 to 10, with "cylinder" includes such deviations from the exact cylinder, the outer perimeter of the cylinder is located in an imaginary tubular space formed by two imaginary exact auxilii cylinders, whereby the diameter of an imaginary inner cylinder is equal to at least 70% of the diameter of an imaginary outer cylinder, an imaginary cylinders are selected so that the ratio of their diameters is most probably close to 1, the diameter of an imaginary outer cylinder is the outer diameter of the geometric the configuration of a hollow cylinder.

2. Reactor system according to claim 1, in which,

when the outer diameter is in the range from 7.4 to 8.6 mm, inner diameter is in the range from 0.1 to less than 3 mm, more specifically from 0.5 to less than 3 mm;

when the outer diameter is in the range of 8.4 to 9.6 mm, inner diameter is in the range from 0.1 to 3.5 mm, more specifically from 0.5 to 3.5 mm;

when the outer diameter is in the range from 9.4 to 106 mm, the internal diameter is in the range from 0.1 to 4.0 mm, more specifically from 0.5 to 4.0 mm;

when the outer diameter is in the range between 10.4 to 11.6 mm, inner diameter is in the range from 0.1 to 3.5 mm, more specifically from 0.5 to 3.5 mm

3. Reactor system containing

an elongated tube having a reaction zone formed by the length and

the diameter of the tube, and the tube diameter is equal to at least 28 mm;

within the reaction zone contains a compacted layer of molded material carrier having a geometrical configuration of a hollow cylinder, a certain nominal length nominal outside diameter and nominal internal diameter so that

the ratio of nominal length nominal outside diameter is in the range from 0.5 to 2 and

the ratio of the nominal outside diameter to the nominal inner diameter provides a positive test result, as hereinafter defined, and additionally so that

the ratio of tube diameter to the nominal outside diameter is in the range from 2 to 10;

where "positive test result" is determined by the decrease of the ratio of the numerical values of pressure drop per unit length of the compacted layer and the numerical values of the packing density, and numerical data the e values are obtained by testing of the compacted layer in a turbulent flow of gaseous nitrogen at a pressure of 1,136 MPa (150 psig) in relation to the comparative ratio of the numerical values, obtained in an identical manner, except that the geometric configuration of the hollow cylinder of the same material of the carrier is determined by the ratio of nominal length nominal external diameter equal to 1;

moreover, "cylinder" includes such deviations from the exact cylinder that, when the outer perimeter of the cylinder is located in an imaginary tubular space formed by two imaginary exact auxilii cylinders, whereby the diameter of an imaginary inner cylinder is equal to at least 70% of the diameter of an imaginary outer cylinder, an imaginary cylinders are selected so that the ratio of their diameters is most probably close to 1, the diameter of an imaginary outer cylinder is the outer diameter of the geometric configuration of a hollow cylinder.

4. Reactor system according to claim 3, in which the geometrical configuration of the hollow cylinder is determined so that the ratio of the nominal outside diameter to the nominal internal diameter exceeding 2.7.

5. Reactor system according to any one of claims 1 to 4, in which

the tube diameter is in the range from 28 to 60 mm and

the ratio of the nominal outside diameter to the nominal inner diameter equal to

at least 4,5, when the outer diameter is inter the ale between 10.4 to 11.6 mm, or

more than 3.4, when the outer diameter is in the range from 9.4 to 10.6 mm, or

at least 2,6, when the outer diameter is in the range of 8.4 to 9.6 mm

6. Reactor system according to claim 5, in which the ratio of the nominal outside diameter to the nominal inner diameter equal to

at least 4,5, when the outer diameter is in the range between 10.4 to 11.6 mm, or

at least 3,6, when the outer diameter is in the range from 9.4 to 10.6 mm, or

is in the range from 2.6 to 7.3, when the outer diameter is in the range of 8.4 to 9.6 mm

7. Reactor system according to claim 1, in which the tube diameter is equal to approximately 39 mm

8. Reactor system according to claim 1, in which the inner diameter of the geometric configuration of a hollow cylinder is equal to at least 0.5 mm

9. Reactor system according to claim 1, in which the ratio of the nominal outside diameter to the nominal internal diameter is in the range from 3.0 to 500.

10. Reactor system according to claim 9, in which the ratio of the nominal outside diameter to the nominal internal diameter is in the range from 3.3 to 250.

11. Reactor system according to claim 1, in which the tube length is in the range from 3 to 15 meters

12. Reactor system according to claim 1, where at least 50% of the compacted layer contains a molded material media.

13. Reactor system according to claim 1, in which the ratio of tube diameter to the nominal outside diameter is in the range from 2.5 to 7.5.

14. Reactor system according to item 13, in which the ratio of tube diameter to the nominal outside diameter is in the range from 3 to 7.

15. Reactor system according to claim 1, in which the molded material of the carrier contains mainly alpha-alumina and a compacted layer has a density packaging tube,big 550 kg/m3.

16. Reactor system according to claim 1, in which the molded material of the carrier is the basis of the catalytic component.

17. Reactor system according to clause 16, in which the catalytic component contains silver.

18. Method for the production of ethylene oxide comprising the steps are carried out:

providing a reactor system according to item 16 or 17, where the elongated tube has an input end of the tube and the output end of the tube;

introduction in the input end of the tube feedstock containing ethylene and oxygen; and

the output from the output end of the tube of the reaction product containing ethylene oxide and unreacted ethylene, if any.

19. The method according to p, in which the reaction zone support suitable conditions the oxidation reaction of ethylene, comprising a temperature in the range from 150 to 400°and a pressure in the range from 0.15 to 3 MPa.

20. SP who own use of ethylene oxide to obtain ethylene glycol, simple ether of ethylene glycol or 1,2-alkanolamine, including the conversion of ethylene oxide to ethylene glycol, a simple ether of ethylene glycol or 1,2-alkanolamine, in which the ethylene oxide receive through method of producing ethylene oxide by p or 19.

21. The catalyst containing silver-based molded material of the carrier, which has a geometric configuration of a hollow cylinder defined by the nominal length nominal outside diameter and nominal internal diameter, so

the ratio of nominal length nominal outside diameter is in the range from 0.5 to 2, and

the ratio of the nominal outside diameter to the nominal internal diameter exceeding 2.7.



 

Same patents:

FIELD: chemistry, pharmaceutics.

SUBSTANCE: invention relates to method of obtaining olefin oxide including interaction of initial mixture, which contains olefin and oxygen, in presence of silver-containing catalyst. According to claimed method, before catalyst reaches late stage of ageing, temperature of reaction is supported higher than 255°C, and content of olefin in initial mixture is supported within the range from higher than 25 mol % to at most 80 mol %, relative to general initial mixture, said reaction temperature and said olefin content being supported, at least, during period which is sufficient to obtain olefin oxide in amount 1000 kmole of olefin oxide per m3 of catalyst layer. "Late stage of ageing" of catalyst is determined by obtaining total olefin oxide in amount, at least, 10000 kmole of olefin oxide per m3 of catalyst layer. Invention also relates to method of obtaining 1,2-diole, ether, 1,2-diole or alkanolamine.

EFFECT: increase of functional performance of silver-containing catalyst.

10 cl, 3 tbl, 10 ex

FIELD: chemistry.

SUBSTANCE: catalyst contains silver, applied on profiled carrier with geometric configuration in form of hollow cylinder, in which ratio of length to outer diameter lies within interval from 0.3 to 2, and inner diameter constitutes up to 30% of outer diameter of said profiled carrier with assumption that when carrier contains more than one channel, inner diameter is considered to be the diameter of one channel with area of transverse section equal to the sum of areas of transverse sections of all channels. Described is method which includes obtaining profiled carrier with geometric configuration in form of hollow cylinder described above, and application of silver on profiled carrier. Described is method of obtaining ethylene oxide which includes: contacting under suitable epoxidation conditions of raw material flow, containing ethylene and oxygen, with described above catalyst. Also described is method of obtaining ethylene glycol, ethylene glycol ester, or 1,2-alkanolamine, which includes using ethylene oxide obtained by described above method and its conversion to ethylene glycol, ethylene glycol ester or 1,2-alaknolamine.

EFFECT: increase of initial activity and stable activity.

18 cl, 4 tbl, 4 ex, 3 dwg

FIELD: chemistry.

SUBSTANCE: catalyst contains carrier and silver, applied on carrier, in amount of at least, 10 g/kg with respect to catalyst weight, where carrier has specific surface area of at least 1.4 m2/g and such pore distribution by size, that pores with diameter in interval from 0.2 to 10 mcm constitute more than 85% of general pore volume, and such pores together form pore volume of at least 0.27 ml/g with respect to carrier weight; method of catalyst obtaining and method of olefin epoxidation, which includes interaction of olefin with oxygen in presence of said catalyst.

EFFECT: high activity and selectivity of catalyst.

21 cl, 2 tbl, ex

FIELD: chemistry.

SUBSTANCE: claimed is water solution of hydrogen peroxide, suitable for olefine epoxidation, which includes: I) in total less than 50 wt fraction/mln of alkaline metals, alkaline-earth metals or their combinations irrespective of whether said alkaline or alkaline-earth metals are in catione-active or complex form; II) in total at least 50 wt fraction/mln of amines, which have pkb value less than 4.5, or respective protonated compounds; and III) in total at least 100 wt fraction/mln anions or compounds, which are able to dissociate with anion formation, according to which values in wt fraction/mln are given in terms of hydrogen peroxide weight. Claimed is method of obtaining hydrogen peroxide solution. Claimed is application of water solution of hydrogen peroxide.

EFFECT: economically efficient production of water solution of hydrogen peroxide and improved long-term activity and selectivity of catalyst.

18 cl, 5 ex, 2 tbl

FIELD: chemistry.

SUBSTANCE: according to the present invention, ethylene is oxidised in contact with mix of heterogeneous catalyst in particles and solid inert substance in particles, treated with alkali metal, in oxidation conditions.

EFFECT: improved efficiency.

3 cl, 1 tbl, 8 ex

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EFFECT: increase in the selectivity of the catalyst.

6 cl, 2 tbl, 7 ex

FIELD: chemistry.

SUBSTANCE: invention pertains to ethylene oxide and to the method of obtaining 1,2-ethanediol or a simple ether of 1,2-ethanediol, from ethylene oxide, obtained using the proposed method. The process of producing ethylene oxide involves an epoxidation reactor system, containing a volume of a high octane epoxidation catalyst. The method involves replacing part of the volume of the high octane epoxidation catalyst with a volume of highly selective catalyst and modification of the process system so as to provide for initial raw materials of the reactor of the epoxidation system, with low concentration of carbon dioxide.

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13 cl, 5 dwg, 5 tbl, 3 ex

FIELD: chemistry.

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22 cl, 8 tbl, 3 ex

FIELD: chemistry.

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EFFECT: increasing of selectivity, activity and stability of catalyst.

10 cl, 5 tbl, 37 ex

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: method of improving selectivity of highly selective epoxidation catalyst on support containing silver in amount at most 0.19 g per 1 m2 of the support surface area comprises bringing catalyst or catalyst precursor containing silver in cationic form into contact with oxygen-containing raw material at catalyst temperature above 250°C over a period of time more than 150 h, after which catalyst temperature is lowered to at most 250°C. Olefin epoxidation process comprises bringing above-described supported catalyst or catalyst precursor into contact with oxygen-containing raw material at catalyst temperature above 250°C over a period of time more than 150 h, after which catalyst temperature is lowered to at most 250°C and catalyst is brought into contact with raw material containing olefin and oxygen.

EFFECT: increased selectivity of catalyst.

12 cl, 3 tbl, 12 ex

FIELD: chemistry.

SUBSTANCE: catalyst contains silver, applied on profiled carrier with geometric configuration in form of hollow cylinder, in which ratio of length to outer diameter lies within interval from 0.3 to 2, and inner diameter constitutes up to 30% of outer diameter of said profiled carrier with assumption that when carrier contains more than one channel, inner diameter is considered to be the diameter of one channel with area of transverse section equal to the sum of areas of transverse sections of all channels. Described is method which includes obtaining profiled carrier with geometric configuration in form of hollow cylinder described above, and application of silver on profiled carrier. Described is method of obtaining ethylene oxide which includes: contacting under suitable epoxidation conditions of raw material flow, containing ethylene and oxygen, with described above catalyst. Also described is method of obtaining ethylene glycol, ethylene glycol ester, or 1,2-alkanolamine, which includes using ethylene oxide obtained by described above method and its conversion to ethylene glycol, ethylene glycol ester or 1,2-alaknolamine.

EFFECT: increase of initial activity and stable activity.

18 cl, 4 tbl, 4 ex, 3 dwg

FIELD: chemistry.

SUBSTANCE: catalytic composition contains compounds of formula: Mo1VaSbbNbcMdOx, in which Mo represents molybdenum, V stands for vanadium, Sb stands for antimony, Nb stands for niobium, M represents gallium, a constitutes from 0.01 to 1, b constitutes from 0.01 to 1, c constitutes from 0.01 to 1, d constitutes from 0.01 to 1, and x is determined by requirements of valency of other present elements.

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9 cl, 1 tbl, 12 ex

FIELD: chemistry.

SUBSTANCE: catalyst for glyoxal synthesis includes silicon-containing silver carrier and silver as active component, as silicon-containing carrier silicate with open pores is used. Ion-conducting modifier, in amount 0.5÷50.0% of catalyst weight, is introduced into silicate pores, silver with particle size 1÷200 nm in amount 1.0÷10.0% of catalyst weight is placed in pore mouths on outer surface of carrier. Also described is method of glyoxal synthesis, including oxidation of ethylene glycol with oxygen, which is in mixture of air with inert gas and water vapours, on silver catalyst at temperature from 450 to 800°C, ethylene glycol oxidation being carried out with reaction mixture, in which molar ratio of oxygen to ethylene glycol is set in interval from 0.7:1.0 to 2.0:1.0, using described above catalyst.

EFFECT: increase of selectivity of ethylene glycol oxidation process, increase of catalyst service term, increase of its heat resistance and reduction of silver consumption for catalyst preparation.

2 cl, 2 tbl, 4 dwg, 10 ex

FIELD: chemistry.

SUBSTANCE: method of preparation of the catalyst of synthesis ethylene oxide is described, constituting of silver on the carrier from aluminium oxide which was processed by the main aqueous solution of salt at temperature below 100°C, and the pH of the aqueous for processing was kept above 8 during processing.

EFFECT: high activity and selectivity of the catalyst.

4 cl, 8 tbl, 17 ex

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: method of improving selectivity of highly selective epoxidation catalyst on support containing silver in amount at most 0.19 g per 1 m2 of the support surface area comprises bringing catalyst or catalyst precursor containing silver in cationic form into contact with oxygen-containing raw material at catalyst temperature above 250°C over a period of time more than 150 h, after which catalyst temperature is lowered to at most 250°C. Olefin epoxidation process comprises bringing above-described supported catalyst or catalyst precursor into contact with oxygen-containing raw material at catalyst temperature above 250°C over a period of time more than 150 h, after which catalyst temperature is lowered to at most 250°C and catalyst is brought into contact with raw material containing olefin and oxygen.

EFFECT: increased selectivity of catalyst.

12 cl, 3 tbl, 12 ex

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to a method of preparing ethylene oxide production catalyst containing silver deposited on alumina carrier originally having sodium and silicate ions on its surface. Carrier is preliminarily treated with aqueous solution of lithium salt at temperature below 100°C, after which at least 25% sodium ions are removed and replaced with up to 10 mln-1 lithium ions. Carrier is dried and then silver and promoters are precipitated on the pretreated and dried carrier.

EFFECT: achieved stability of catalyst.

7 cl, 11 tbl, 17 ex

FIELD: organic synthesis.

SUBSTANCE: invention relates to olefin epoxidation method and methods for preparing 1,2-diol or 1,2-diol ether, or alkylamine including conversion of olefin oxide into 1,2-diol or 1,2-diol ether, or alkylamine. Olefin epoxidation method comprises: (a) preliminarily impregnating high-selectivity silver-based epoxidation catalyst with organohalogen compound; (b) passing, over preliminarily impregnated catalyst, a material free of organohalogen compound or containing it in concentration not higher than 2·10-4 mol % (calculated for halogen) over a period of time from 15 h to 200 h; and (c) contacting resulting catalyst with material containing olefin, oxygen, and organohalogen compound wherein concentration of organohalogen compound is by at least 0.2·10-4 mol % higher than that of compound in step (b). Preparation of 1,2-diol, 1,2-diol ether, or alkylamine is also described.

EFFECT: optimized process parameters.

13 cl, 1 tbl

FIELD: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: invention relates to catalytic compositions palladium/silver on carrier, to methods for preparation thereof, and to unsaturated hydrocarbon hydrogenation processes. catalytic composition containing platinum, silver, and iodine component (options) is described as well as methods for preparation thereof comprising interaction of composition containing palladium, silver, and carrier with liquid composition containing iodine component followed by calcination. Alternatively, carrier is brought into consecutive interaction with palladium component, silver component, and iodine component using intervals for intermediate calcination after each interaction. Hydrocarbon hydrogenation process is also described, in particular selective hydrocarbon of acetylene into ethylene, in presence of above-defined catalytic composition.

EFFECT: increased hydrogenation process selectivity and reduced degree of catalyst deactivation.

52 cl, 1 tbl, 6 ex

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention provides catalyst for oxidation of ethylene into ethylene oxide, which catalyst contains no rhenium and no transition metals and comprises up to 30% silver on solid support and promoter combination mainly consisted of (i) component containing alkali metal on amount from 700 to 3000 ppm of the mass of catalyst and (ii) component containing sulfur in amount from 40 to 100% by weight of amount required to form alkali metal sulfate and, optionally, a fluorine-containing component in amount from 10 to 300 ppm of the mass of catalyst. Ethylene oxide is produced via reaction of ethylene with molecular oxygen in presence of above-defined catalyst.

EFFECT: increased selectivity of catalyst.

9 cl, 3 tbl

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention provides catalyst for production of glyoxal via catalytic oxidation of ethylene glycol, wherein lower catalyst bed is composed of crystalline copper, upper bed of fibrous silver granules, and the two beds are modified with phosphorus. Crystalline copper particles are 1 to 100 μm in pore size and 5 to 50 μm in wall thickness. Fibrous silver granules are 0.01 to 3.00 mm in size with their specific surface being between 0.10 and 0,17 m2/g. Surface concentration of phosphorus is between 0.1 and 6% for lower bed and between 0.05 and 3.00% for upper one.

EFFECT: increased conversion and selectivity of ethylene glycol oxidation process and simplified catalyst bed formation.

4 cl, 4 ex

FIELD: catalysts.

SUBSTANCE: invention relates to novel catalyst fillings containing physical mixture of catalytically active and catalytically inactive molded particles wherein catalytically inactive molded particles have rounded edges on their friction surfaces.

EFFECT: reduced mechanical wear inside catalytic filling and preserved low pressure drop over the filling.

2 cl

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