CN111905657B - A large-scale synthesis gas to ethylene glycol reactor - Google Patents

Abstract

The invention relates to a large-scale reactor for preparing ethylene glycol from synthesis gas, which comprises: the reactor body comprises an upper end enclosure, a cylinder and a lower end enclosure which are integrally formed; the inside center of barrel is located to gas collection unit (9) axial, for top confined cavity component, includes: a gas collecting cylinder, the cylinder wall of which is provided with a plurality of through holes, the through holes are dense at the top and sparse at the bottom, and are small at the top and big at the bottom, and a product outlet (5) which is integrally arranged at the bottom end of the gas collecting cylinder and is positioned on the lower end enclosure; the heat exchange tube bundle (8) is axially arranged between the gas collection unit (9) and the inner wall of the cylinder; a plurality of groups of raw material inlets (1) are arranged on the upper end enclosure and/or the cylinder in pairs; the heat exchange medium outlet (6) and the at least one heat exchange medium inlet (4) are respectively arranged on the upper end enclosure and the lower end enclosure and are communicated with the heat exchange tube bundle (8); the catalyst bed layer (2) is distributed among the heat exchange tube bundles (8). Compared with the prior art, the catalyst layer has small pressure drop and low operation cost.

Description

A large-scale synthesis gas to ethylene glycol reactor

technical field

The invention relates to a ethylene glycol preparation reactor, in particular to a large-scale synthesis gas-to-ethylene glycol reactor.

Background technique

The carbonylation reactor and the hydrogenation reactor are one of the core equipment of the synthesis gas to ethylene glycol plant. The reactions of synthesis gas to oxalate and oxalate hydrogenation to ethylene glycol are all exothermic reactions. For the carbonylation reaction, which is a fast reaction of the second order, the reaction is mainly concentrated in the upper part of the catalyst tube, the lower part plays a balancing role, and the heat removal of the bed mainly depends on the heat exchange area in the upper part of the catalyst tube; in an emergency, the reaction Heat builds up, the catalyst bed is over-temperature, and the nitrite is thermally decomposed, which can easily cause an explosion accident. Since the hydrogenation anti-catalyst is easy to coke and pulverize, the resistance of each catalyst tube in the reactor is different, and gas bias flow occurs, the catalyst bed is partially overheated, the side reactants are high, and the catalyst utilization rate is low; The pressure drop is large, and the power consumption of the compressor is high.

At present, the carbonylation reactor and hydrogenation reactor in operation and in design are both tubular reactors. Under the same transportation conditions, the catalyst loading of a single reactor is small, and the operating resistance of the reaction system is reduced. For a 200,000-ton/year ethylene glycol plant, 2 carbonylation reactors and 3 to 4 hydrogenation reactors are usually required, which not only covers a large area, but also has high engineering cost, which is easy to cause gas bias and difficult to operate. The specifications of the reactor of a single set of 200,000 tons/year dimethyl oxalate production unit have been selected to have a diameter of 6m and a height of 8m, which brings many problems in transportation, installation and operation. The tubular reactor has limited the development of large-scale .

In order to save energy, reduce consumption and save investment, the scale of newly installed ethylene glycol units has become larger and larger, and some have reached one million tons. The development of large-scale therefore requires the development of reactors suitable for large or ultra-large plants.

Patent CN204911449U discloses a novel carbonylation reactor for the synthesis gas to ethylene glycol process. The reactor is a radial reactor, including a reactor shell, a heat exchange assembly, a branch pipe, a collector pipe and a catalyst. The tube is located in the center of the reactor, the heat exchange component is arranged between the shunt tube and the header, the heat exchange component is arranged in the catalyst bed, and the reactor shell includes a cylinder, an upper head, a lower head, a reaction gas inlet, and a reaction gas inlet. The gas outlet, cooling medium inlet, cooling medium outlet and catalyst discharge port, etc.; the reaction gas inlet and the reaction gas outlet are all set on the upper head, and the reaction gas enters the reactor from the reaction gas inlet and flows down the central shunt pipe, radially The reaction proceeds through the catalyst bed, and the reaction product gas enters the header, flows upward along the header, and exits the outlet of the reaction gas. Although this reactor is used to prepare ethylene glycol from syngas, it still cannot solve the problem of large pressure drop in the device, and this reactor can only be used for carbonylation reaction, not for hydrogenation reaction.

SUMMARY OF THE INVENTION

The purpose of the present invention is to provide a large-scale synthesis gas-to-ethylene glycol reactor in order to solve the above problems.

The object of the present invention is achieved through the following technical solutions:

A large-scale synthesis gas-to-ethylene glycol reactor comprising:

a reactor body, including a top-to-bottom integrally formed

Once you put the cover on,

a barrel and

head off;

A gas collecting unit, axially arranged in the inner center of the cylinder, is a hollow member with a closed top, including:

A gas collecting cylinder body, the cylinder wall of the gas collecting cylinder body is provided with

a plurality of through holes, the through holes are dense on the top and sparse on the bottom, small on the top and large on the bottom, and

a product outlet, integrally provided at the bottom end of the gas collecting cylinder body, and located on the lower head;

a heat exchange tube bundle, axially arranged between the gas collecting unit and the inner wall of the cylinder;

Multiple groups of raw material inlets are arranged in pairs on the upper head and/or the outer wall of the cylinder;

At least one heat exchange medium inlet is arranged on the lower head and communicated with the heat exchange tube bundle;

a heat exchange medium outlet, arranged on the upper head, and communicated with the heat exchange tube bundle; and

A catalyst bed is distributed between the heat exchange tube bundles.

Further, the through holes are circular holes or vertical strip holes, which play the role of controlling the pressure drop distribution.

Further, the heat exchange tube bundle is selected from straight tubes, serpentine coils or pipes with straight tubes at both ends of the serpentine coil in the middle.

Further, the tube outer diameter of the heat exchange tube bundle is 15-55 mm, and the tube center distance is 25-100 mm.

Further, the reactor is also provided with a gas distributor between the cylinder and the heat exchange tube bundle, an annular gap for gas flow is provided between the gas distributor and the cylinder wall, and the gas distributor includes a gas distribution pipe and A through hole on the gas distribution pipe. Further optimally, the gas distribution pipe is a 1/4 ring, which is beneficial to the uniform distribution of the raw material gas in the reactor cylinder.

Further, a catalyst frame is provided on the side of the gas distributor and the gas collecting cylinder body close to the catalyst bed, and a stainless steel wire mesh is provided on the catalyst frame to facilitate the fixing of the catalyst.

Further, the diameter of the cylinder body is 3000-8000mm, and the height is 4000-12000mm.

A large-scale synthesis gas-to-ethylene glycol reactor, when using the reactor for reaction, the raw material enters the reactor from the raw material inlet, flows radially through the catalyst bed and reacts, the product reaches the gas gathering unit, and flows out from the product outlet ; Boiler feed water enters the heat exchange tube bundle through the heat exchange medium inlet, exchanges heat with the raw materials and products of the reaction, turns into high temperature boiling water or steam, and then flows out from the heat exchange medium outlet.

The invention adopts a gas collecting unit, and the through holes on the cylinder wall of the gas collecting cylinder body of the gas collecting unit are in the shape of upper dense and lower sparse, upper small and lower large. It is designed according to the properties of reaction raw materials and products such as alcohol; the radial reactor is used, the catalyst loading is large, and the pressure drop of the catalyst bed is small; the radial temperature difference of the radial reactor is small, which is conducive to the full and effective utilization of the catalyst, Reduce the temperature of the catalytic bed and prolong the service life of the catalyst; by feeding the raw gas in multiple stages, the distribution of the raw gas is strengthened, and the pressure drop of the bed is improved at the same time.

Compared with the prior art, the present invention has the following beneficial effects:

The invention not only has the advantages of general radial reactors, such as saving the energy consumption of the device, reducing the operating cost, etc.; but also overcomes the shortcomings of the large-scale fixed-bed reactor that is difficult to manufacture and transport, and can reduce the operating cost, and the reactor can fully adapt to large-scale fixed-bed reactors. Syngas-to-ethylene glycol plant.

Description of drawings

Fig. 1 is the structural representation of a kind of large-scale synthesis gas to ethylene glycol reactor;

Fig. 2 is a bottom sectional view of a large-scale chemical synthesis gas-to-ethylene glycol reactor;

Fig. 3 is the schematic diagram of the material flow direction when the present invention is used to carry out the reaction.

In the figure: I-upper head; II-cylinder; III-lower head; 1-raw material inlet; 2-catalyst bed; 3-gas distributor; 4-heat exchange medium inlet; 5-product outlet; 6 - outlet of heat exchange medium; 7 - catalyst frame; 8 - heat exchange tube bundle; 9 - gas collection unit; a - raw material; b - product; c - boiler feed water; d - high temperature boiling water or steam.

Detailed ways

The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.

Example 1

A large-scale synthesis gas-to-ethylene glycol reactor comprising:

a reactor body, including a top-to-bottom integrally formed

Once you put on the cover I,

A Cylinder II and

next head III;

A gas collecting unit 9, axially arranged in the inner center of the cylinder II, is a hollow member with a closed top, including:

A gas collecting cylinder body, the cylinder wall of the gas collecting cylinder body is provided with

A number of through holes, the upper part of the through hole is dense and the lower part is sparse, the upper part is small and the lower part is large, and

A product outlet 5 is integrally arranged at the bottom end of the gas collecting cylinder body, and is located on the lower head III;

A heat exchange tube bundle 8 is axially arranged between the gas collecting unit 9 and the inner wall of the cylinder II;

Multiple groups of raw material inlets 1 are arranged in pairs on the outer wall of the upper head I and/or the cylinder II;

At least one heat exchange medium inlet 4 is arranged on the lower head III and communicated with the heat exchange tube bundle 8;

A heat exchange medium outlet 6, arranged on the upper head 1, and communicated with the heat exchange tube bundle 8; and

A catalyst bed 2 is distributed between the heat exchange tube bundles 8 .

Through holes are round holes or vertical strip holes.

The heat exchange tube bundle 8 selects a straight tube, a serpentine coil or a pipe with a serpentine coil in the middle and straight tubes at both ends.

The reactor is further provided with a gas distributor 3 between the cylinder body II and the heat exchange tube bundle 8, and the gas distributor 3 includes a gas distribution pipe and a through hole provided on the gas distribution pipe. The gas distribution pipe is a 1/4 ring.

A catalyst frame 7 is arranged on the side of the gas distributor 3 and the gas collecting cylinder body close to the catalyst bed, and a stainless steel wire mesh is arranged on the catalyst frame 7 .

A large-scale synthesis gas-to-ethylene glycol reactor, when using the reactor for reaction, the raw material a enters the reactor from the raw material inlet 1, flows radially through the catalyst bed 2 and reacts, and the product b reaches the gas gathering unit 9 , flows out from the product outlet 5; the boiler feed water c enters the heat exchange tube bundle 8 through the heat exchange medium inlet 4, and exchanges heat with the reacted raw materials a and product b to become high-temperature boiling water or steam d and then flows out from the heat exchange medium outlet 6.

The reactor was used for the carbonylation reaction, the height of the cylinder II was DN 8000mm, the diameter was DN 4600mm, the outer diameter of the heat exchange tubes in the heat exchange tube bundle was 30mm, the heat exchange tubes were arranged in a regular triangle shape, the tube center distance was 48mm, and the catalyst filled The installed volume is greater than 120m ³ , the normal load operation is performed, the production capacity of dimethyl oxalate is greater than 400kt/a, and the pressure drop of the catalyst bed is less than 15kPa.

Example 2

A large-scale synthesis gas-to-ethylene glycol reactor is specifically described in Example 1, and the reactor is used for carbonylation reaction. The heat exchange tube is 30mm, the heat exchange tubes are arranged in an equilateral triangle, the tube center distance is 48mm, the catalyst packing volume is greater than 200m ³ , the normal load operation, the dimethyl oxalate production capacity is greater than 600kt/a, and the catalyst bed pressure drop is less than 18kPa.

Example 3

A large-scale synthesis gas-to-ethylene glycol reactor is specifically described in Example 1, and the reactor is used for carbonylation reaction. The heat exchange tube is 28mm, the heat exchange tubes are arranged in an equilateral triangle, the tube center distance is 44mm, the catalyst filling volume is greater than 270m ³ , the normal load operation, the dimethyl oxalate production capacity is greater than 900kt/a, and the catalyst bed pressure drop is less than 18kPa.

Example 4

A large-scale synthesis gas-to-ethylene glycol reactor is specifically as described in Example 1. The reactor is used for carbonylation reaction. The heat exchange tube is 30mm, the heat exchange tubes are arranged in an equilateral triangle, the tube center distance is 48mm, the catalyst filling volume is greater than 60m ³ , the normal load operation, the dimethyl oxalate production capacity is greater than 200kt/a, and the catalyst bed pressure drop is less than 13kPa.

Example 5

A large-scale synthesis gas-to-ethylene glycol reactor is specifically described in Example 1. The reactor is used for hydrogenation reaction. The height of the cylinder II is DN 4000mm, the diameter is DN 4000mm, and the outer diameter of the heat exchange tube in the heat exchange tube bundle is DN 4000mm. The heat exchange tube is 25mm, the heat exchange tubes are arranged in an equilateral triangle, the tube center distance is 44mm, the catalyst packing volume is greater than 55m ³ , the normal load operation, the ethylene glycol production capacity is greater than 100kt/a, and the catalyst bed pressure drop is less than 25kPa.

Example 6

A large-scale synthesis gas-to-ethylene glycol reactor is specifically described in Example 1, and the reactor is used for hydrogenation reaction. 30mm, the heat exchange tube is a serpentine coil, the tube center distance is 50mm, the catalyst filling volume is greater than 110m ³ , the normal load operation, the ethylene glycol production capacity is greater than 200kt/a, and the catalyst bed pressure drop is less than 30kPa.

Example 7

A large-scale synthesis gas-to-ethylene glycol reactor is specifically as described in Example 1. The reactor is used for hydrogenation reaction. DN 4200mm, the outer diameter of the heat exchange tubes in the heat exchange tube bundle is 28mm, the heat exchange tubes are arranged in an equilateral triangle, the tube center distance is 48mm, the catalyst filling volume is greater than 110m ³ , the normal load operation, the ethylene glycol production capacity is greater than 200kt/a , the catalyst bed pressure drop is less than 28kPa.

Example 8

A large-scale synthesis gas-to-ethylene glycol reactor is specifically as described in Example 1. The reactor is used for hydrogenation reaction. The height of the cylinder II is DN 9000mm, the diameter is DN 4600mm, and the outer diameter of the heat exchange tube in the heat exchange tube bundle is DN 9000mm. The heat exchange tube is 30mm, the heat exchange tubes are arranged in an equilateral triangle, the tube center distance is 52mm, the catalyst filling volume is greater than 165m ³ , the normal load operation, the ethylene glycol production capacity is greater than 300kt/a, and the catalyst bed pressure drop is less than 30kPa.

Example 9

A large-scale synthesis gas-to-ethylene glycol reactor is specifically described in Example 1. The reactor is used for hydrogenation reaction. The height of the cylinder II is DN 12000mm, the diameter is DN 5800mm, and the outer diameter of the heat exchange tube in the heat exchange tube bundle is DN 12000mm. The heat exchange tube is 16mm, the heat exchange tubes are arranged in an equilateral triangle, the tube center distance is 25mm, the catalyst filling volume is greater than 245m ³ , the normal load operation, the ethylene glycol production capacity is greater than 450kt/a, and the catalyst bed pressure drop is less than 35kPa.

The foregoing description of the embodiments is provided to facilitate understanding and use of the invention by those of ordinary skill in the art. It will be apparent to those skilled in the art that various modifications to these embodiments can be readily made, and the generic principles described herein can be applied to other embodiments without inventive step. Therefore, the present invention is not limited to the above-mentioned embodiments, and improvements and modifications made by those skilled in the art according to the disclosure of the present invention without departing from the scope of the present invention should all fall within the protection scope of the present invention.

Claims (9)

1. The large-scale synthesis gas ethylene glycol preparation reactor is characterized by comprising:

a reactor body integrally formed from top to bottom

An upper end enclosure (I) is arranged on the upper end enclosure,

a cylinder (II) and

a lower end enclosure (III);

a gas collection unit (9), the axial is located barrel (II) inside center, for the closed cavity component in top, includes:

a gas collecting cylinder body, the cylinder wall of which is provided with a gas collecting cylinder

A plurality of through holes with dense top and sparse bottom, small top and large bottom, an

A product outlet (5) which is integrally arranged at the bottom end of the gas collecting cylinder body and is positioned on the lower seal head (III);

the heat exchange tube bundle (8) is axially arranged between the gas collection unit (9) and the inner wall of the cylinder body (II);

the raw material inlets (1) are arranged on the top of the upper end enclosure (I) and the outer wall of the middle lower part of the cylinder body (II) in pairs;

the at least one heat exchange medium inlet (4) is arranged on the lower end socket (III) and communicated with the heat exchange tube bundle (8);

the heat exchange medium outlet (6) is arranged on the upper end enclosure (I) and communicated with the heat exchange tube bundle (8); and

and the catalyst bed layer (2) is distributed among the heat exchange tube bundles (8).

2. The reactor for preparing ethylene glycol from large-scale synthesis gas as claimed in claim 1, wherein the through holes are round holes or vertical strip holes.

3. The large-scale reactor for preparing glycol from synthesis gas according to claim 1, wherein the heat exchange tube bundle (8) is a straight tube, a serpentine coil or a tube with a serpentine coil in the middle and straight tubes at two ends.

4. The reactor for preparing ethylene glycol from large-scale synthesis gas according to claim 3, wherein the heat exchange tube bundle (8) has an outer tube diameter of 15-55 mm and a tube center distance of 25-100 mm.

5. The large-scale synthesis gas ethylene glycol reactor according to claim 1, wherein a gas distributor (3) is further disposed between the cylinder (II) and the heat exchange tube bundle (8), and the gas distributor (3) comprises a gas distribution pipe and through holes disposed on the gas distribution pipe.

6. The large-scale reactor for producing ethylene glycol from synthesis gas as claimed in claim 5, wherein the gas distribution pipe is 1/4 circular ring.

7. The large-scale reactor for preparing glycol from synthesis gas according to claim 5, wherein a catalyst frame (7) is arranged on one side of the gas distributor (3) and the gas collecting cylinder body close to the catalyst bed layer, and a stainless steel wire mesh is arranged on the catalyst frame (7).

8. The reactor for preparing ethylene glycol from large-scale synthesis gas according to claim 1, wherein the diameter of the cylinder (II) is 3000-8000 mm, and the height is 4000-12000 mm.

9. The large-scale synthesis gas ethylene glycol reactor according to any one of claims 1-8, wherein when the reactor is used for reaction, raw materials (a) enter the reactor from a raw material inlet (1), flow radially through the catalyst bed (2) and react, and products (b) reach a gas collecting unit (9) and flow out from a product outlet (5); boiler feed water (c) enters a heat exchange tube bundle (8) through a heat exchange medium inlet (4), exchanges heat with the raw material (a) and the product (b) of the reaction to become high-temperature boiling water or steam (d), and then flows out from a heat exchange medium outlet (6).

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