RU2719441C1 - Reactor for large-scale synthesis of ethylene glycol - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: disclosed is a reactor for large-scale production of dimethyl oxalate from carbon monoxide (CO) and methylnitrite (MN), where one of the embodiments comprises: (a) housing with internal walls (M) of reactor cylinder, wherein said housing forms upper part (I), reactor cylinder (II) and lower part (III); (b) a gas distribution element comprising one or more inlet feed pipes (A) for feeding initial gas, one or more gas distribution amplifiers (G), having gas distributor pores (D), hollow gas cylinder (L) with gas cylinder walls having holes, as well as one or more tail gas discharge branch pipes (F); (c) an internal heat exchange element comprising a bundle (J) of heat exchange tubes; (d) two or more inlet pipe elements equipped with two or more boiler water supply connection pipes (E); and (e) two or more outlet pipe elements equipped with two or more outlet branch pipes (H) for discharging boiling water at high temperature; in which each of said two or more inlet pipe elements corresponds to one of two or more outlet pipe elements, and each inlet pipe element and its corresponding outlet pipe element are located symmetrically around the circumference on lower part (III) and upper part (I), respectively, or on lower part and upper part of cylinder (II), respectively; in which one or more inlet branch pipes (A) of source gas supply, one or several gas distribution amplifiers (G), as well as at least two of two or more outlet pipe elements are located in upper part (I); in which one or more tail gas discharge branch pipes (F), as well as at least two of two or more inlet pipe elements are located in lower part (III); in which gas distributor (D), bundle (J) of heat exchange tubes, catalyst layer (C), as well as gas cylinder (L) are in reactor cylinder (II); wherein catalyst layer (C) is located between gas distributor (D) and gas cylinder (L) and outside of bundle (J) of heat exchange tubes, and also comprises catalyst; in which bundle (J) of heat exchange tubes is located between gas distributor (D) and gas cylinder (L) and provides a pipe channel for continuously flowing boiler water from two or more inlet pipes (E) supply of boiler water to two or more outlet nozzles (H) discharge of boiling water at high temperature, and also performs heat removal; wherein internal walls of reactor cylinder, pores in gas distributor (D) and holes in gas cylinder (L) provide spatial channel for continuous flow of initial gas from one or more inlet nozzles (A) feeding the feed gas to one or more tail gas discharge branch pipes (F), as well as contacting the feed gas with the catalyst in the presence of the removed heat; in which holes in walls of gas cylinder (L) are configured to provide pressure drop in catalyst layer of less than 30 kPa; and in which the starting gas contains carbon monoxide (CO) and methylnitrite (MN), and the catalyst catalyses a process of synthesis of dimethyl oxalate from carbon monoxide (CO) and methylnitrite (MN), wherein the desired product is dimethyl oxalate, and said reactor has dimethyl oxalate productivity of more than 400 kt/year. Also disclosed is a device for large-scale production of dimethyl oxalate from carbon monoxide (CO) and methylnitrite (MN), a device for large-scale production of ethylene glycol from dimethyl oxalate and hydrogen (H2), method of producing dimethyl oxalate from carbon monoxide (CO) and methylnitrite (MN) on a large scale in a reactor, a method of producing ethylene glycol from dimethyl oxalate and hydrogen (H2) on a large scale in a reactor.

EFFECT: technical result is overcoming problems associated with large-scale production of dimethyloxylate synthesis by carbonylation and/or ethylene glycol via hydrogenation in gas phase, by proposing a reactor capable of effectively reducing pressure drop in reactor and associated with working unit.

22 cl, 4 ex, 2 dwg

Description

FIELD OF THE INVENTION

This invention relates to the synthesis of ethylene glycol in the gas phase, especially on a large scale.

BACKGROUND OF THE INVENTION

The carbonylation reactor and the hydrogenation reactor are key components of the equipment necessary for the synthesis of ethylene glycol from synthesis gas. Both the synthesis of oxalate from synthesis gas by carbonylation and the synthesis of ethylene glycol from oxalate by hydrogenation is an exothermic reaction. The carbonylation reaction is a quick reaction lasting a few seconds, and it occurs mainly in the upper part of the catalytic tube, while its lower part provides equilibrium when removed from the catalyst layer, depending mainly on the heat exchange zone in the upper part of the catalytic tube. In an emergency, reaction heat accumulates, and the catalyst layer overheats so much that nitrite decomposes under the influence of heat, which can easily lead to an explosion. During the hydrogenation reaction, the catalyst is easily coked and crumbles, which leads to different resistance in each of the catalytic tubes of the reactor. As a result, gas drift occurs, the catalyst layer undergoes local overheating, side reactions amplify and the catalyst utilization rate decreases. This causes a sharp drop in pressure in the catalyst bed. The compressor consumes much more electricity.

Both the carbonylation reactors and the hydrogenation reactors currently in operation and currently being designed are tubular reactors. Under identical conditions of transportation, the loading of one reactor with a catalyst is negligible, and the resistance in the reaction unit is reduced. To create a plant for the production of ethylene glycol with a capacity of 200,000 tons / year or 200 kt / year, as a rule, it is necessary to have two carbonylation reactors and three to four hydrogenation reactors, which not only occupy a large area, but are also very expensive in terms of their construction. In such an installation, gas drift can easily occur, and its operation is difficult. Each of the reactors of a single complex of a plant for the production of dimethyl oxalates with a capacity of 200,000 tons / year can be 6 m in diameter and 8 m in height, thereby causing many problems in the process of transportation, installation and operation. A tubular reactor has limitations when ramping up production to a large scale.

In order to save electricity and reduce investment, newly built ethylene glycol production plants are becoming larger and larger, and some of them have already reached production volumes of millions of tons. Existing tubular carbonylation reactors and hydrogenation reactors limit the expansion of ethylene glycol production to a large scale. Accordingly, there remains a need for ethylene glycol synthesis reactors suitable for large or very large reaction plants.

SUMMARY OF THE INVENTION

The present invention provides a reactor for large-scale production of dimethyl oxalate or ethylene glycol, as well as its scope.

At the same time, a reactor is proposed for large-scale production of the target product.

This reactor contains a housing, a gas distribution element, an internal heat exchange element, inlet pipe elements and exhaust pipe elements. Its body is equipped with inner walls (M) of the reactor cylinder. The specified body forms the upper part (I), the reactor cylinder (II) and the lower part (III). The said gas distribution element comprises one or more inlet nozzles (A) for supplying a source gas, one or more gas distribution amplifiers (G), a pore-distributed gas distributor (D), a hollow gas cylinder (L), and one or more discharge outlet pipes (F) tail gases. Said internal heat exchange element comprises a bundle (J) of heat exchange tubes. Each of said two or more inlet pipe elements is equipped with two or more inlet pipes (E) for supplying boiler water. Each of the two or more exhaust pipe elements mentioned is equipped with two or more exhaust pipes (H) for discharging boiling water at high temperature. Each of these two or more inlet pipe elements corresponds to one of two or more outlet pipe elements. Each inlet tube element and its corresponding outlet tube element are arranged symmetrically in a circle on the lower part (III) and upper part (I), respectively, or on the lower part and upper part of the cylinder (II), respectively.

One or more inlet nozzles (A) for supplying a source gas, one or more gas distribution amplifiers (G), and at least two of two or more outlet pipe elements are located in the upper part (I). One or more tailpipe vents (F), as well as at least two of the two or more inlet tubular elements, are located in the lower part (III). The gas distributor (D), the bundle (J) of the heat transfer tubes, the catalyst bed (C), and the gas cylinder (L) are located in the reactor cylinder (II). The catalyst bed (C) is located between the gas distributor (D) and the gas cylinder (L) and outside the bundle (J) of heat transfer tubes. The catalyst layer contains a catalyst.

The heat exchange tube bundle (J) is located between the gas distributor (D) and the gas cylinder (L) and provides a pipe channel for the continuous flow of boiler water from two or more inlet pipes (E) of the boiler water supply to two or more outlet pipes (N) for boiling discharge at high water temperature. In this case, heat is removed from the beam (J) of the heat exchange tubes.

The inner walls of the reactor cylinder, the pores in the gas distributor (D) and the holes in the gas cylinder (L) provide a spatial channel for a continuous flow of the source gas from one or more inlet pipes (A) of the source gas to one or more outlet pipes (F) of the tail discharge gases so that the source gas is in contact with the catalyst in the presence of heat removed. And if the source gas contains carbon monoxide (CO) and methyl nitrite (MN), then the catalyst catalyzes the synthesis of dimethyl oxalate from carbon monoxide (CO) and methyl nitrite (MN), which is the target product, and this reactor has a dimethyl oxalate capacity of more than 400 ct / year. And if, as an alternative, the source gas contains dimethyl oxalate and hydrogen (H ₂ ), then the catalyst catalyzes the synthesis of ethylene glycol from dimethyl oxalate and hydrogen (H ₂ ), which is the target product, and the indicated reactor has an ethylene glycol capacity of more than 200 ct / year .

In addition, the specified reactor contains a steam drum, which is located in the upper part (I).

Such a reactor may be a radial reactor. The reactor cylinder (II) and gas cylinder (L) of this radial reactor can be arranged vertically. The reactor cylinder (II) and gas cylinder (L) can be on the same vertical axis. The holes in the walls of the gas cylinder may have a higher density in the lower part of the walls of the gas cylinder than in the upper part of its walls. These holes are made in the form of circles or vertical stripes. The porous gas distributor (D) can be separated from the catalyst bed (C) by a catalyst cage (K) made of stainless steel mesh. The gas cylinder (L) can be separated from the catalyst bed (C) by a catalyst cage (K) made of stainless steel mesh. One or more inlet nozzles (A) for supplying the source gas may be located in the upper part (I), and one or more outlet nozzles (F) for discharging the tail gases may be in the lower part (III). The gas cylinder (L) may have a closed upper end.

In a radial reactor, the cylindrical body (II can be connected to the upper part (I)) using the upper flange, while the cylindrical body (II) can be connected to the lower part using the lower flange, and the gas cylinder (L) can have an upper end closed by a gas cylinder flange. Two or more inlets (E) for boiler water (E) may be located on the lower flange.

In addition, the reactor may contain one or more additional reactor cylinders on the reactor cylinder (II), as well as one or more additional gas cylinders on the gas cylinder (L). One or more additional reactor cylinders can be connected to the cylindrical body (II) using an additional flange, and one or more additional gas cylinders are connected to the gas collection cylinder (L) using a gas cylinder flange. As a result, a steam drum is formed between one or more additional cylindrical bodies and a cylindrical body (II).

Said bundle of heat exchange tubes may comprise tubes. Each tube is selected from the group consisting of straight tubes, continuous coils, as well as their combination. The outer diameter of such tubes can be from 15 to 50 mm, and the center distance between them can be from 25 to 90 mm.

The reactor cylinder (II) may have a diameter of from 4000 to 7000 mm and a height of from 2800 to 8000 mm.

The pressure drop in the catalyst bag may be less than 30 kPa. One or more of its catalysts may have a volume in excess of 100 m ³ .

A device is also offered. The device comprises a reactor having an ethylene glycol capacity of more than 200 kt / year, and a single straight tube or a single continuous water cooling coil.

In addition, a method for producing the target product on a large scale in a reactor is proposed.

In accordance with such a method, said reactor comprises a housing, a gas inlet pipe, a gas discharge outlet pipe, a water inlet pipe and a water discharge pipe. The casing forms a vertical reactor cylinder. In the reactor cylinder there are internal cylinder walls, a gas distributor equipped with pores, a catalyst layer, a bundle of heat exchange tubes, and a vertical hollow gas cylinder with openings on the walls of the gas cylinder. The gas cylinder is located in the center of the cylindrical body, and a gas outlet is connected to the gas cylinder. The gas distributor is located between the inner wall of the reactor cylinder and the gas cylinder, and the gas inlet pipe is connected to the space located between the gas distributor and the inner wall of the reactor cylinder. The catalyst layer is located between the gas distributor and the gas cylinder and outside the bundle of heat transfer tubes. The catalyst layer contains a catalyst. The heat exchange tube bundle is located between the gas distributor and the gas cylinder and is connected to the water inlet and the water outlet. The space between the inner wall of the reactor cylinder and the gas distributor, the pores in the gas distributor, and also the openings in the wall of the gas cylinder provide a channel for gas to flow from the gas inlet to the gas outlet.

The specified method includes the supply of boiler water to the inlet pipe of the water supply; continuous movement of the boiler water through the bundle of heat transfer tubes so that this boiler water removes heat from the bundle of heat transfer tubes, and as a result, water and steam boiling at high temperature are formed; discharge of boiling water and steam from a reactor at a high temperature through an outlet pipe for water discharge; supplying source gas to the gas inlet; continuous movement of the source gas through the gas channel; introducing the source gas into contact with the catalyst in the presence of heat removed, as a result of which the target product is obtained and tail gas is formed; and also discharging tail gas from the reactor through the gas outlet.

And if the source gas contains carbon monoxide (CO) and methyl nitrite (MN), and the catalyst catalyzes the synthesis of dimethyl oxalate from carbon monoxide (CO) and methyl nitrite (MN), then the target product is dimethyl oxalate produced by this reactor with a yield of more than 400 ct / year for at least one year. And if, as an alternative, the source gas contains dimethyl oxalate and hydrogen (H ₂ ), and the catalyst catalyzes the synthesis of ethylene glycol from dimethyl oxalate and hydrogen (H ₂ ), then the target product is ethylene glycol produced by the specified reactor with a yield of more than 200 ct / year for at least one year.

In accordance with the method of the invention, the bundle of heat exchange tubes may comprise one or more tubes selected from the group consisting of a straight tube, a continuous coil, and a combination thereof. The outer diameter of one or more tubes can be from 15 to 50 mm, and the center distance between them can be from 25 to 90 mm. The reactor cylinder may have a diameter of 4000 to 7000 mm and a height of 2800 to 8000 mm. The pressure drop in the catalyst bed may be less than 30 kPa. One or more of its catalysts may have a volume in excess of 100 m ³ .

BRIEF DESCRIPTION OF THE DRAWING

In FIG. 1A is a side view of a reactor in accordance with one embodiment of the present invention, and FIG. 1B is a plan view of this reactor. (I) the upper part; (Ii) a cylinder; (Iii) the lower part; A: feed gas inlet B: flange C: catalyst bed D: gas distributor E: boiler water inlet F: gas outlet; G: gas booster; N: exhaust pipe discharge boiling at high temperature water; J: bundle of tubes (straight or serpentine); K: catalyst holder L: gas cylinder; M: inner wall of the cylinder.

In FIG. 2 is a schematic view showing how (1) the source gas enters the reactor, and (2) tail gas leaves the reactor, and how (3) boiler water enters the reactor, and (4) boiling water leaving the reactor leaves the reactor at high temperature and steam.

DETAILED DESCRIPTION OF THE INVENTION

The present invention provides a reactor for the large-scale production of dimethyl oxalate by carbonylation or ethylene glycol by hydrogenation. This invention not only provides the advantages of an ordinary radial reactor, in which the amount of catalyst loading increases, the pressure drop in the catalyst bed decreases, the energy consumption of the working unit is reduced, operating costs are reduced, but the difficulties associated with the production and transportation of a large fixed bed reactor are also overcome. Multiple reactor cylinders and gas cylinders can be used to increase reactor productivity within the desired weight tolerance range and reduce equipment investment; while in the reactor decreases the radial temperature gradient, which favorably affects the completeness and efficiency of the use of catalysts, lowering the temperature of the catalyst layer, extending the life of the catalyst, and also reducing operating costs. For example, in the reactor of the present invention, the pressure drop in the catalyst bed may be less than 30 kPa if the latter is loaded with more than 100 m ^{3 of} catalyst. The reactor can be fully adapted to large-scale ethylene glycol production plants.

One of the objectives of the present invention is to overcome the problems associated with large-scale synthesis of dimethyl oxalate through carbonylation and / or ethylene glycol by hydrogenation in the gas phase, by proposing a reactor that can effectively reduce the pressure drop in the reactor and the associated working unit. For example, as shown in FIG. 1, a large-scale carbonylation radial reactor and hydrogenation consists of a vessel, an internal heat exchange element, a gas distribution element, an inlet pipe element and an exhaust pipe element, wherein the internal heat exchange element contains a bundle of heat exchange tubes, the body forms the upper part (I), the reactor cylinder (II), as well as the lower part (III), and the upper part (I) and the lower part (III), respectively, are equipped with an inlet pipe for gas supply and an outlet pipe for gas discharge. The reactor itself is distinguished by the following: the inlet pipe element and the outlet pipe element, respectively, are located on the lower part (III) and the upper part (I) or in the lower part and the upper part of the reactor cylinder (II) and are located symmetrically to each other around the circumference. Each of the parts (I, III) is equipped with two or more inlet or outlet elements. The feed gas inlet pipe A is equipped with a gas distribution amplifier. A bundle of heat exchanger tubes is located between the porous gas distributor D and gas cylinder L. The upper part (I) is equipped with a boiling water or high-temperature steam discharge nozzle element that serves as a steam drum. The boiler water flows through a bundle J of heat exchange tubes. The catalyst is loaded into the opening between the bundle J of heat transfer tubes, where it forms a catalyst layer. Gas flows through the space between the outer wall of the porous gas distributor D and the inner wall of the gas cylinder. The gas cylinder is located in the center of the reactor cylinder (II). There are holes in the walls of the gas cylinder whose density in the lower part of the walls of the gas cylinder is higher than in the upper part of its walls. These holes are made in the form of circles and reduce the pressure drop. Both the porous gas distributor D and the central gas collection cylinder L are separated from the catalyst bed using a catalyst sleeve K made of stainless steel mesh. The central gas cylinder L is a hollow element, the upper end of which is closed. The reactor cylinder (I) and each of its parts are connected by a flange B. The upper end of the gas cylinder L is closed by a flange. The heat exchanger tube bundle J is a straight pipe, and boiler water is supplied through the inlet pipe E, which is located on the lower flange. In FIG. 2 shows how the feed gas rapidly flows radially from the porous gas distributor D through the catalyst bed C, reaches the gas cylinder L and flows from the lower exhaust gas discharge pipe F. Boiler water follows the specified pipe and flows from the upper outlet pipe F discharge boiling at high temperature water.

A reactor is proposed here to produce the desired product on a large scale. Such a target product may be dimethyl oxalate or ethylene glycol. This reactor consists of a vessel, a gas distribution element, an internal heat exchange element, an inlet pipe element and an exhaust pipe element. The reactor may have a dimethyl oxalate capacity of more than about 400 ct / year, or an ethylene glycol capacity of more than about 200 ct / year.

Its body is equipped with inner walls (M) of the reactor cylinder. The specified housing accommodates the upper part (I), the reactor cylinder (II) and the lower part (III).

The gas distribution element contains an inlet pipe (A) for supplying a source gas through which the source gas enters the reactor; a gas distribution amplifier (G) that enhances the distribution of the source gas in the reactor by, for example, using a fan-like turbofan design that changes the direction of its flow due to the rotation of the gas; a gas distributor (D), in which there are pores, and which distributes the source gas to the catalysts in the catalyst bed, passing the source gas through its pores and directing it into the hollow gas cylinder (L), in which there are openings. Tail gas accumulates in the hollow gas cylinder and is discharged from the reactor through the tail gas discharge outlet (F).

Said internal heat exchange element consists of a bundle (J) of heat exchange tubes. The specified inlet pipe element is equipped with two or more inlet nozzles (E) for supplying boiler water. The outlet pipe element is equipped with an outlet pipe (N) for discharging boiling water at high temperature.

Each inlet pipe element corresponds to a specific outlet pipe element. Each inlet tube element and its corresponding outlet tube element are arranged symmetrically in a circle on the lower part (III) and upper part (I), respectively, or the lower part and upper part of the cylinder (II), respectively.

The inlet pipe (A) for supplying the source gas, the gas distribution booster (G), as well as at least two exhaust pipe elements are located in the upper part (I). The gas distributor (D), the bundle (J) of the heat transfer tubes, the catalyst bed (C), and the gas cylinder (L) are located in the reactor cylinder (II). The tail gas discharge outlet (F) and at least two inlet pipe elements are located in the lower part (III).

The catalyst bed (C) is located between the gas distributor (D) and the gas cylinder (L), but outside the bundle (J) of the heat exchange tubes. The catalyst layer contains a catalyst.

Between the gas distributor (D) and the gas cylinder (L) there is a bundle (J) of heat exchange tubes, which provides a pipe channel for a continuous flow of boiler water from the inlet pipe (E) of the supply to the outlet pipe (H) of the discharge of boiling water at high temperature. In this case, heat is removed from the beam (J) of the heat exchange tubes.

The inner walls of the reactor cylinder, the pores in the gas distributor (D) and the holes in the gas cylinder (L) provide a spatial channel for a continuous flow of the source gas from the inlet pipe (A) of the source gas to the outlet pipe (F) of the tail gas discharge so that the source the gas contacts the catalysts in the presence of heat removed.

And if the source gas contains carbon monoxide (CO) and methyl nitrite, then the catalyst catalyzes the synthesis of dimethyl oxalate from carbon monoxide (CO) and methyl nitrite, which is the target product, and this reactor may have a dimethyl oxalate capacity of more than 400, 500, 600, 700 or 800 ct / year.

And if, as an alternative, the source gas contains dimethyl oxalate and hydrogen (H ₂ ), and the catalyst catalyzes the synthesis of ethylene glycol from dimethyl oxalate and hydrogen (H ₂ ), then the target product is ethylene glycol, and this reactor may have an ethylene glycol capacity of more than 100, 150, 200, 250, 300, 350, 400, 450 or 500 ct / year. In addition, the specified reactor is equipped with a steam drum, which is located in the upper part (I).

Such a reactor may be a radial reactor. The reactor cylinder (II) and gas cylinder (L) of this radial reactor can be arranged vertically. The reactor cylinder (II) and gas cylinder (L) can be on the same vertical axis. The holes in the walls of the gas cylinder can have a higher density in the lower part of the walls of the gas cylinder than in the upper part of its walls, and these holes are made in the form of circles or vertical stripes. The porous gas distributor (D) can be separated from the catalyst bed (C) by a catalyst cage (K) made of stainless steel mesh. The gas cylinder (L) can be separated from the catalyst bed (C) by a catalyst cage (K) made of stainless steel mesh. The source gas inlet (A) may be located in the upper part (I), and the tail gas outlet (F) in the lower part (III). The gas cylinder (L) may have a closed upper end.

The cylindrical body (II) of the radial reactor can be connected to the upper part (I) using the upper flange, while this cylindrical body (II) can be connected to the lower part using the lower flange, and the gas cylinder (L) of such a reactor can have upper end closed by gas cylinder flange. Two or more boiler water inlets (E) may be located at the bottom flange.

In addition, the reactor, in addition to the reactor cylinder (II), can be equipped with an additional reactor cylinder. Such an additional reactor cylinder may be connected to the cylindrical body (II) using an additional flange. The gas collection cylinder (L) can be connected using the gas cylinder flange. As a result, a steam drum may be formed between one or more additional cylindrical bodies and a cylindrical body (II).

Said bundle of heat exchange tubes may comprise tubes. Each of the tubes can be selected from the group consisting of a straight tube, a continuous coil, as well as their combination. The inner diameter of such tubes can be from about 15 to 50 mm, and the center distance between them is from about 25 to 90 mm.

The reactor cylinder (II) may have a diameter of from about 4000 to 7000 mm and / or a height of from about 2800 to 8000 mm.

The pressure drop in the catalyst bed may be less than about 5, 10, 12, 15, 20, 25, 30 kPa. The volume of one or more catalysts may exceed about 100, 110, 120,130,140, 150, 160, 170,180,190 or 200 m ³ .

A device for large-scale production is also offered here. Such a device comprises the reactor of the present invention, as well as a single straight tube or a single continuous coil of a water cooling system.

In addition, a method for producing the target product on a large scale in a reactor is proposed. The specified reactor contains a housing, an inlet pipe for supplying gas, an outlet pipe for discharging gas, an inlet pipe for supplying water and an outlet pipe for discharging water. The casing forms a vertical reactor cylinder. In the reactor cylinder there are internal cylinder walls, a gas distributor equipped with pores, a catalyst layer, a bundle of heat exchange tubes, and a vertical hollow gas cylinder with openings having walls. The gas cylinder is located in the center of the cylindrical body, and a gas outlet is connected to the gas cylinder. The gas distributor is located between the inner wall of the reactor cylinder and the gas cylinder, and the gas inlet pipe is connected to the space located between the gas distributor and the inner wall of the reactor cylinder. The catalyst layer and the bundle of heat transfer tubes are located between the gas distributor and the gas cylinder and outside the bundle of heat transfer tubes. The catalyst layer contains a catalyst. The heat exchange tube bundle is connected to the water inlet pipe and the water discharge pipe, and also provides a pipe channel for water to flow from the water inlet pipe to the water discharge pipe. The space between the inner wall of the reactor cylinder and the gas distributor, the pores in the gas distributor, and also the holes in the walls of the gas cylinder provide a channel for gas to flow from the gas inlet to the gas outlet.

The specified method includes the supply of boiler water to the inlet pipe of the water supply; continuous movement of the boiler water through the bundle of heat transfer tubes so that this boiler water removes heat from the bundle of heat transfer tubes, and as a result, water and steam boiling at high temperature are formed; discharge of boiling water and steam from a reactor at a high temperature through an outlet pipe for water discharge; supplying source gas to the gas inlet; continuous movement of the source gas through the gas channel; introducing the source gas into contact with the catalyst in the presence of heat removed, as a result of which the target product is obtained and tail gas is formed; and also discharging tail gas from the reactor through the gas outlet.

And if the source gas contains carbon monoxide (CO) and methyl nitrite (MN), and the catalyst catalyzes the synthesis of dimethyl oxalate from carbon monoxide (CO) and methyl nitrite (MN), the target product is dimethyl oxalate, which is produced by this reactor with a yield of more than 400, 500 , 600. 700 or 800 ct / year for at least one year. And if, as an alternative, the source gas contains dimethyl oxalate and hydrogen (H ₂ ), and the catalyst catalyzes the synthesis of ethylene glycol from dimethyl oxalate and hydrogen (H ₂ ), then the target product is ethylene glycol, which is produced by the specified reactor with a yield of more than 100, 150, 200, 250, 300, 350, 400, 450 or 500 ct / year for at least one year. According to the technology of the invention, the bundle of heat exchange tubes may comprise tubes. Each of these tubes is selected from the group consisting of a straight tube, a continuous coil, as well as their combination. The inner diameter of such tubes can be from about 15 to 50 mm, and the center distance between them is from about 25 to 90 mm. The reactor cylinder may have a diameter of from about 4000 to 7000 mm and / or a height of from about 2800 to 8000 mm. The pressure drop in the catalyst bed may be less than about 5, 10, 12, 15, 20, 25, 30 kPa. The volume of one or more catalysts may exceed about 100, 110, 120, 130, 140, 150, 160, 170,180, 190 or 200 m ³ .

The term “about”, as used herein when referring to a measured value, for example, quantity, percent, and the like, is intended to encompass deviations within ± 20% or ± 10%, more preferably ± 5%, even more preferably ± 1 % and even more preferably ± 0.1% of the indicated value, since such deviations correspond to the norm.

Sample 1.

A carbonylation reactor was used, equipped with two reactor cylinders with a height of DN 4000 mm and a diameter of DN 4600 mm. The outer diameter of the heat transfer tubes in the bundle of heat transfer tubes was 28 mm, and they were arranged in the form of a positive triangle, and the center distance between the tubes was 44 mm. The catalyst was filled in a volume exceeding 120 m ³ . Under normal operating conditions, the dimethyl oxalate capacity exceeded 400 ct / year. The pressure drop in the catalyst bed was less than 12 kPa.

Sample 2.

A carbonylation reactor was used, equipped with two reactor cylinders with a height of DN 4000 mm and a diameter of DN 5800 mm. The outer diameter of the heat transfer tubes in the bundle of heat transfer tubes was 28 mm, and they were arranged in the form of a positive triangle, and the center distance between the tubes was 44 mm. The catalyst was filled in a volume exceeding 200 m ³ . Under normal operating conditions, the dimethyl oxalate capacity exceeded 600 ct / year. The pressure drop in the catalyst bed was less than 12 kPa.

Sample 3.

A hydrogenation reactor was used, equipped with two reactor cylinders with a height of DN 4000 mm and a diameter of DN 4000 mm. The outer diameter of the heat transfer tubes in the bundle of heat transfer tubes was 25 mm, and they were arranged in the form of a positive triangle, and the center distance between the tubes was 44 mm. The catalyst was filled in a volume exceeding 110 m ³ . Under normal operating conditions, ethylene glycol capacity exceeded 200 ct / year. The pressure drop in the catalyst bed was less than 30 kPa.

Sample 4.

A hydrogenation reactor was used, equipped with two reactor cylinders with a height of DN 5000 mm and a diameter of DN 4400 mm. The outer diameter of the heat transfer tubes in the bundle of heat transfer tubes was 25 mm, and they were arranged in the form of a positive triangle, and the center distance between the tubes was 44 mm. The catalyst was filled in a volume exceeding 162 m ³ . Under normal operating conditions, ethylene glycol capacity exceeded 300 ct / year. The pressure drop in the catalyst bed was less than 30 kPa.

Although the claimed invention is illustrated and described herein with reference to specific embodiments, it is not limited to the demonstrated characteristics. Conversely, various changes may be made to these characteristics within the scope and range of equivalents of the claims without departing from the invention itself.

Claims (67)

1. A reactor for large-scale production of dimethyl oxalate from carbon monoxide (CO) and methyl nitrite (MN), containing: (a) a casing with inner walls (M) of the reactor cylinder, said casing forming the upper part (I), the reactor cylinder (II) and the lower part (III); (b) a gas distribution element comprising one or more inlet pipes (A) for supplying a source gas, one or more gas distribution amplifiers (G), a pore-shaped gas distribution valve (D), a hollow gas cylinder (L) with openings on the walls of the gas cylinder, and one or more tailpipe vents (F); (c) an internal heat exchange element comprising a bundle (J) of heat transfer tubes; (d) two or more inlet pipe elements equipped with two or more inlet pipes (E) for supplying boiler water; as well as (e) two or more outlet pipe elements equipped with two or more outlet pipes (H) for discharging boiling water at high temperature; in which each of these two or more inlet pipe elements corresponds to one of two or more outlet pipe elements, and each inlet pipe element and its corresponding outlet pipe element are located symmetrically around the circumference on the lower part (III) and the upper part (I), respectively or on the lower and upper parts of the cylinder (II), respectively; in which one or more inlet nozzles (A) for supplying the source gas, one or more amplifiers (G) of gas distribution, as well as at least two of the two or more exhaust pipe elements are located in the upper part (I); in which one or more exhaust pipes (F) discharge tail gases, as well as at least two of the two or more inlet pipe elements are located in the lower part (III); in which the gas distributor (D), the bundle (J) of the heat exchange tubes, the catalyst bed (C), as well as the gas cylinder (L) are in the reactor cylinder (II); in which the catalyst layer (C) is located between the gas distributor (D) and the gas cylinder (L) and outside the bundle (J) of heat exchange tubes, and also contains a catalyst; in which the bundle (J) of heat exchange tubes is located between the gas distributor (D) and the gas cylinder (L) and provides a pipe channel for a continuous flow of boiler water from two or more inlet pipes (E) of the boiler water supply to two or more outlet pipes (H) discharge boiling water at high temperature, and also carries out heat dissipation; in which the inner walls of the reactor cylinder, the pores in the gas distributor (D) and the holes in the gas cylinder (L) provide a spatial channel for a continuous flow of the source gas from one or more inlet nozzles (A) of the source gas to one or more outlet nozzles (F) tail gas discharge, as well as contacting the source gas with the catalyst in the presence of heat removed; in which the holes in the walls of the gas cylinder (L) are configured to provide a pressure drop in the catalyst layer of less than 30 kPa; and in which the source gas contains carbon monoxide (CO) and methyl nitrite (MN), and the catalyst catalyzes the synthesis of dimethyl oxalate from carbon monoxide (CO) and methyl nitrite (MN), the target product being dimethyl oxalate, and said reactor has a dimethyl oxalate capacity of more than 400 ct /year. 2. A reactor for large-scale production of ethylene glycol from dimethyl oxalate and hydrogen (H ₂ ), containing: (a) a casing with inner walls (M) of the reactor cylinder, said casing forming the upper part (I), the reactor cylinder (II) and the lower part (III); (b) a gas distribution element comprising one or more inlet pipes (A) for supplying a source gas, one or more gas distribution amplifiers (G), a pore-shaped gas distribution valve (D), a hollow gas cylinder (L) with openings on the walls of the gas cylinder, and one or more tailpipe vents (F); (c) an internal heat exchange element comprising a bundle (J) of heat transfer tubes; (d) two or more inlet pipe elements equipped with two or more inlet pipes (E) for supplying boiler water; as well as (e) two or more outlet pipe elements equipped with two or more outlet pipes (H) for discharging boiling water at high temperature; in which each of these two or more inlet pipe elements corresponds to one of two or more outlet pipe elements, and each inlet pipe element and its corresponding outlet pipe element are located symmetrically around the circumference on the lower part (III) and the upper part (I), respectively or on the lower and upper parts of the cylinder (II), respectively; in which one or more inlet nozzles (A) for supplying the source gas, one or more amplifiers (G) of gas distribution, as well as at least two of the two or more exhaust pipe elements are located in the upper part (I); in which one or more exhaust pipes (F) discharge tail gases, as well as at least two of the two or more inlet pipe elements are located in the lower part (III); in which the gas distributor (D), the bundle (J) of the heat exchange tubes, the catalyst bed (C), as well as the gas cylinder (L) are in the reactor cylinder (II); in which the catalyst layer (C) is located between the gas distributor (D) and the gas cylinder (L) and outside the bundle (J) of heat exchange tubes, and also contains a catalyst; in which the bundle (J) of heat exchange tubes is located between the gas distributor (D) and the gas cylinder (L) and provides a pipe channel for a continuous flow of boiler water from two or more inlet pipes (E) of the boiler water supply to two or more outlet pipes (H) discharge boiling water at high temperature, and also carries out heat dissipation; in which the inner walls of the reactor cylinder, the pores in the gas distributor (D) and the holes in the gas cylinder (L) provide a spatial channel for a continuous flow of the source gas from one or more inlet nozzles (A) of the source gas to one or more outlet nozzles (F) tail gas discharge, as well as contacting the source gas with the catalyst in the presence of heat removed; in which the holes in the walls of the gas cylinder (L) are configured to provide a pressure drop in the catalyst layer of less than 30 kPa; and in which the source gas contains dimethyl oxalate and hydrogen (H ₂ ), the catalyst catalyzes the synthesis of ethylene glycol from dimethyl oxalate and hydrogen (H ₂ ), the target product being ethylene glycol, and the indicated reactor has an ethylene glycol capacity of more than 200 ct / year. 3. The reactor according to claim 1 or 2, further comprising a steam drum in the upper part (I). 4. The reactor according to claim 1 or 2, wherein said reactor is a radial reactor in which the reactor cylinder (II) and the gas cylinder (L) are arranged vertically. 5. The reactor according to claim 4, in which the holes in the walls of the gas cylinder have a higher density in the lower part of the walls of the gas cylinder than in the upper part of its walls, and such holes are made in the form of circles or vertical stripes. 6. The reactor according to claim 4, in which the porous gas distributor (D) is separated from the catalyst layer (C) by a catalyst holder (K) made of stainless steel mesh. 7. The reactor according to claim 4, in which the gas cylinder (L) is separated from the catalyst layer (C) by a catalyst holder (K) made of stainless steel mesh. 8. The reactor according to claim 4, in which one or more inlet pipes (A) for supplying the source gas are located in the upper part (I), and one or more exhaust pipes (F) for discharging the tail gases are located in the lower part (III). 9. The reactor according to claim 4, in which the gas cylinder (L) has a closed upper end. 10. The reactor according to claim 4, in which the cylindrical body (II) is connected to the upper part (I) using the upper flange, while the cylindrical body (II) is connected to the lower part using the lower flange, and the gas cylinder (L) has upper end closed by gas cylinder flange. 11. The reactor according to claim 10, in which two or more inlet pipes (E) of the boiler water supply are located on the lower flange. 12. The reactor according to claim 1 or 2, further comprising one or more additional reactor cylinders on the reactor cylinder (II), as well as one or more additional gas cylinders on the gas cylinder (L), wherein one or more additional reactor cylinders are connected to a cylindrical body (II) using an additional flange, and one or more additional gas cylinders are connected to the gas collection cylinder (L) using a gas cylinder flange, and as a result between one or more additional and a cylindrical bodies and a cylindrical body (II) forms a steam drum. 13. The reactor according to claim 1 or 2, in which the specified bundle of heat exchange tubes contains tubes, each of which is selected from the group consisting of a straight tube, a continuous coil, as well as combinations thereof, the outer diameter of the tubes is from 15 to 50 mm, and the center distance between them is from 25 to 90 mm. 14. The reactor according to claim 1 or 2, in which the reactor cylinder (II) has a diameter of from 4000 to 7000 mm and a height of from 2800 to 8000 mm. 15. The reactor according to claim 1 or 2, in which one or more catalysts have a volume exceeding 100 m ³ . 16. A device for the large-scale production of dimethyl oxalate from carbon monoxide (CO) and methyl nitrite (MN), containing the reactor according to claim 1 and a single straight pipe or a single continuous water cooling coil. 17. A device for the large-scale production of ethylene glycol from dimethyl oxalate and hydrogen (H ₂ ), containing the reactor according to claim 2 and a single straight tube or a single continuous water cooling coil. 18. A method for the production of dimethyl oxalate from carbon monoxide (CO) and methyl nitrite (MN) on a large scale in a reactor in which the reactor comprises a vessel, a gas inlet, a gas outlet, a water inlet, and a water outlet; moreover, the housing forms a vertical reactor cylinder; in the reactor cylinder there are internal walls of the cylinder, a gas distributor equipped with pores, a catalyst layer, a bundle of heat exchange tubes, and a vertical hollow gas cylinder with openings on the walls of the gas cylinder; a gas cylinder is located in the center of the cylindrical body, and a gas outlet is connected to the gas cylinder; a gas distributor is located between the inner wall of the reactor cylinder and the gas cylinder, and the gas inlet pipe is connected to a space located between the gas distributor and the inner wall of the reactor cylinder; the catalyst layer is located between the gas distributor and the gas cylinder and outside the bundle of heat transfer tubes, and also contains a catalyst; moreover, the bundle of heat transfer tubes is located between the gas distributor and the gas cylinder and is connected to the inlet pipe of the water supply and the outlet pipe of the water discharge; and the space between the inner wall of the reactor cylinder and the gas distributor, the pores in the gas distributor, and also the holes in the wall of the gas cylinder provide a channel for gas to flow from the gas inlet to the gas outlet, while the openings in the walls of the gas cylinder are designed to provide a differential pressure in a catalyst layer of less than 30 kPa, this method includes: (a) supplying boiler water to the water inlet; (b) continuous movement of boiler water through a bundle of heat exchange tubes, as a result of which this boiler water removes heat from the bundle of heat exchange tubes, and water and steam boiling at high temperature are formed; (c) discharging boiling water and steam from a reactor at a high temperature through a water outlet; (d) supplying a source gas to a gas inlet; (e) continuous movement of the source gas through the gas channel; (f) introducing the source gas into contact with the catalyst in the presence of heat removed, whereby the desired product is obtained and tail gas is formed; as well as (g) discharging tail gas from the reactor through a gas outlet; in which the source gas contains carbon monoxide (CO) and methyl nitrite (MN), and the catalyst catalyzes the synthesis of dimethyl oxalate from carbon monoxide (CO) and methyl nitrite (MN), and the target product is dimethyl oxalate, which is continuously produced in the specified reactor with a yield of more than 400 ct / year for at least one year. 19. A method for the production of ethylene glycol from dimethyl oxalate and hydrogen (H ₂ ) on a large scale in a reactor in which the reactor comprises a body, a gas inlet pipe, a gas outlet pipe, a water inlet pipe and a water discharge pipe; moreover, the housing forms a vertical reactor cylinder; in the reactor cylinder there are internal walls of the cylinder, a gas distributor provided with pores, a catalyst layer, a bundle of heat exchange tubes, and also a vertical hollow gas cylinder with openings on the walls of the gas cylinder; a gas cylinder is located in the center of the cylindrical body, and a gas outlet is connected to the gas cylinder; a gas distributor is located between the inner wall of the reactor cylinder and the gas cylinder, and the gas inlet pipe is connected to a space located between the gas distributor and the inner wall of the reactor cylinder; the catalyst layer is located between the gas distributor and the gas cylinder and outside the bundle of heat transfer tubes, and also contains a catalyst; moreover, the bundle of heat transfer tubes is located between the gas distributor and the gas cylinder and is connected to the inlet pipe of the water supply and the outlet pipe of the water discharge; and the space between the inner wall of the reactor cylinder and the gas distributor, the pores in the gas distributor, and also the holes in the wall of the gas cylinder provide a channel for gas to flow from the gas inlet to the gas outlet, while the openings in the walls of the gas cylinder are designed to provide a differential pressure in a catalyst layer of less than 30 kPa, this method includes: (a) supplying boiler water to the water inlet; (b) continuous movement of boiler water through a bundle of heat exchange tubes, as a result of which this boiler water removes heat from the bundle of heat exchange tubes, and water and steam boiling at high temperature are formed; (c) discharging boiling water and steam from a reactor at a high temperature through a water outlet; (d) supplying a source gas to a gas inlet; (e) continuous movement of the source gas through the gas channel; (f) introducing the source gas into contact with the catalyst in the presence of heat removed, whereby the desired product is obtained and tail gas is formed; as well as (g) discharging tail gas from the reactor through a gas outlet; in which the source gas contains dimethyl oxalate and hydrogen (H ₂ ), and the catalyst catalyzes the synthesis of ethylene glycol from dimethyl oxalate and hydrogen (H ₂ ), and the target product is ethylene glycol, which is continuously produced in the specified reactor with a yield of more than 200 ct / year over at least one year. 20. The method according to p. 18 or 19, in which the specified bundle of heat transfer tubes contains one or more tubes selected from the group consisting of a straight tube, continuous coil, as well as combinations thereof, the outer diameter of the specified one or more tubes is from 15 to 50 mm, and the center distance between them is from 25 to 90 mm. 21. The method according to p. 18 or 19, in which the reactor cylinder has a diameter of from 4000 to 7000 mm and a height of from 2800 to 8000 mm 22. The method according to p. 18 or 19, in which one or more catalysts have a volume exceeding 100 m ³ .

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