KR200491359Y1 - A hydromechanical reactor - Google Patents

Abstract

This utility model relates to a type of hydrodynamic reactor, wherein the hydrodynamic reactor is a vertical cylindrical configuration comprising a cylindrical portion (1), an upper enclosure (2) and a lower enclosure (3), and the lower enclosure (3). Is a curved enclosure extending downward, wherein the hydrodynamic reactor comprises a liquid inlet (4), a liquid nozzle (5), a gas outlet (6), a baffle (7), a gas inlet (8), a gas distributor (9), And a liquid outlet (10): the liquid inlet (4) is located at the top of the hydrodynamic reactor, and at a radial center at or near the top of the cylindrical portion (1) of the hydrodynamic reactor. Is connected to a liquid nozzle 5 which is located and configured to discharge the liquid in the downward direction; The gas outlet 6 is located in the upper enclosure of the hydrodynamic reactor; The baffle (7) is located radially centered in the lower enclosure (3) of the hydrodynamic reactor, the baffle (7) being above the horizontal base element (11), the horizontal base element (11) A vertical peripheral wall (12) extending inwardly, and an angled peripheral wall (13) connecting the horizontal base element (11) and the vertical peripheral wall (12); The gas inlet 8 is located at the bottom of the hydrodynamic reactor and is connected to the gas distributor 9; The gas distributor 9 is: radially centered within the diameter drawn by the vertical peripheral wall 12 of the baffle 7 and not lower than the horizontal base element 11 and also the vertical peripheral wall ( 12) is positioned vertically at a position not higher than the upper portion of the; Or in a diameter drawn by the vertical peripheral wall 12 of the baffle 7 and located vertically in the radial center and above the vertical peripheral wall 12 and the gas distributor 9 is connected to the baffle ( 7) is configured to expel the gas towards the volume defined within; The liquid outlet (10) is located in the radial center at the bottom of the lower enclosure (3) of the hydrodynamic reactor; The ratio of the diameter (D) of the cylindrical portion 1 of the hydrodynamic reactor to the height B of the cylindrical portion 1 of the hydrodynamic reactor is in the range of 1.5: 1 to 1: 3, and the hydrodynamics The ratio of the height B of the cylindrical portion 1 of the hydrodynamic reactor to the overall height C of the reactor ranges from 1: 1 to 1: 3; The ratio of the radius N of the horizontal base element 11 of the baffle 7 to the radius 0 of the vertical peripheral wall 12 of the baffle 7 ranges from 0.3: 1 to 0.95: 1 , And the ratio of the height J of the vertical peripheral wall 12 of the baffle 7 to the radius 0 of the vertical peripheral wall 12 of the baffle 7 is 1:15 to 1: 5 Is the range of; The baffle 7 is provided so that a first gap K is provided between the edge where the vertical peripheral wall 12 and the angled peripheral wall 13 meet and the inner surface of the lower enclosure 3 and the angled The second gap (L) is positioned between the peripheral wall (13) and the edge where the horizontal base element (11) meets and the inner surface of the lower enclosure (3), the distance of the first gap (K) The ratio of the diameter D of the cylindrical portion 1 of the hydrodynamic reactor to the range of 10: 1 to 60: 1, and the cylindrical portion of the hydrodynamic reactor to the distance of the second gap L The ratio of the diameter (D) of 1) ranges from 10: 1 to 80: 1.

Description

Hydrodynamic reactor {A HYDROMECHANICAL REACTOR}

This utility model relates to the type of hydrodynamic reactor.

The use of carbonylation of methanol and / or its reaction derivatives in the presence of a rhodium or iridium based catalyst system is well known and is commonly used worldwide in the production of acetic acid. The production of acetic acid by carbonylation of methanol and / or reaction derivatives thereof in the presence of a rhodium catalyst is disclosed, for example, in GB-A-1,233,121, EP 0384652, and EP 0391680. Processes in the presence of iridium catalysts are disclosed, for example, in GB-A-1234641, US-A-3772380, EP 0616997, EP 0618184, EP 0786447, EP 0643034, EP 0752406. In these processes for producing acetic acid, the carbonylation reaction is carried out in the liquid phase and thus requires mixing of the liquid phase methanol and / or its reaction derivatives and gaseous carbon monoxide reactants. Typically, mechanical approaches to mixing in reactors have been adopted to achieve complete gas-liquid and liquid-liquid mixing, but due to the large amount of corrosive components present during the acetic acid synthesis process, high levels of corrosion are mechanically It affects the seals of rotating machinery and mixing equipment, causing damage to the mixing equipment and disruption of the equipment, potentially causing problems with continuous operation. From this point of view, a need has emerged for the improvement of reactors of new construction that can achieve good gas / liquid mixing results for use in acetic acid synthesis.

CN 203209061 U discloses a type of hydrodynamic reactor, wherein the hydrodynamic reactor comprises a gas outlet, baffle, liquid spray module, gas inlet, gas distributor, liquid outlet and liquid inlet; The gas inlet is located on the side from the bottom of the reactor, the gas outlet is located on the top of the reactor, the liquid inlet is located on the base of the reactor, and the liquid outlet symmetrically arranged on the two sides of the bottom cover of the reactor There are; The gas distributor is located between the baffle and the liquid spray module; The baffle is located under the top cover of the reactor; The baffle has gas outlet vent openings. The configuration of the reactor provided in CN 203209061 U may result in less than ideal mixing of gas and liquid on a baffle pan, which may lead to a reduction of carbon monoxide on the baffle, and also carbonization after carbon monoxide is dissolved in the liquid phase. Before having sufficient residence time to be consumed by the reaction, there is the potential for the upward flow of both liquid and gas to induce carbon monoxide to escape from the surface of the liquid reaction medium. The concentration of carbon monoxide in the liquid reaction medium is reduced to minimize or even eliminate portions of the reaction volume where the carbonylation reaction cannot occur and / or sufficient to be consumed in the carbonylation reaction after the carbon monoxide is dissolved in the liquid phase. There is still a need for a reactor configuration that achieves good mixing to minimize or even eliminate carbon monoxide emissions through the surface of the liquid reaction medium at or near the top of the reactor prior to having a residence time.

The technical problems associated with the prior art to be solved by this utility model are poor gas / liquid mixing results and poor gas residence time in the liquid reaction medium. The reactor provided by this utility model is intended to achieve good gas / liquid mixing and also maximize residence time of gas and gas phase dissolved in the liquid reaction medium.

In order to solve the above technical problems, the technical schema of the utility model includes a type of hydrodynamic reactor, wherein the reactor includes a cylindrical portion 1, an upper enclosure 2 and a lower enclosure 3 in the vertical direction. Cylindrical construction, the lower enclosure 3 is a curved enclosure extending downward, and the reactor comprises a liquid inlet 4, a liquid nozzle 5, a gas outlet 6, a baffle 7, a gas inlet 8 ), A gas distributor (9), and a liquid outlet (10):

-The liquid inlet (4) is located at the top of the reactor, and at the top of or near the cylindrical portion of the reactor (1), a radial center and a liquid nozzle configured to discharge the liquid in a downward direction (5);

-The gas outlet 6 is located in the upper enclosure of the reactor;

-The baffle (7) is located in a radial center in the lower enclosure (3) of the reactor, the baffle (7) extends upwardly with respect to the horizontal base element (11), the base element (11) A vertical peripheral wall (12), and an angled peripheral wall (13) connecting the horizontal base element (11) and the vertical peripheral wall (12);

-The gas inlet (8) is located at the bottom of the reactor and is connected to the gas distributor (9);

-The gas distributor 9 is: radially centered in a diameter drawn by the vertical peripheral wall of the baffle 7 and not lower than the horizontal base element 11 and also the vertical peripheral wall 12 Vertically located at a position not higher than the upper portion of the; Or in a diameter drawn by the vertical peripheral wall of the baffle (7) radially centered and vertically above the top of the vertical peripheral wall (12) and the gas distributor (9) in the baffle (7) Configured to expel gas towards a defined volume;

-The liquid outlet 10 is located in the radial center at the bottom of the lower enclosure 3 of the reactor;

-The ratio of the diameter (D) of the cylindrical portion (1) of the reactor to the height (B) of the cylindrical portion (1) of the reactor is in the range of 1.5: 1 to 1: 3, and the overall height (C) of the reactor The ratio of the height B of the cylindrical portion 1 of the reactor to the range of 1: 1 to 1: 3;

The ratio of the radius N of the horizontal base element 11 of the baffle 7 to the radius 0 of the vertical peripheral wall 12 of the baffle 7 is in the range of 0.3: 1 to 0.95: 1 , The ratio of the height J of the vertical peripheral wall 12 of the baffle 7 to the radius 0 of the vertical peripheral wall 12 of the baffle 7 is in the range of 1:15 to 1: 5 ;

The baffle 7 is provided so that a first gap K is provided between the edge where the vertical peripheral wall 12 and the angled peripheral wall 13 meet and the inner surface of the lower enclosure 3 and the angled peripheral wall 13 ) And the cylindrical portion of the reactor relative to the distance of the first gap (K), which is positioned to provide a second gap (L) between the edge where the horizontal base element (11) meets and the inner surface of the lower enclosure (3). The ratio of the diameter D of 1) ranges from 10: 1 to 80: 1, and the ratio of the diameter D of the cylindrical portion 1 of the reactor to the distance of the second gap L is 10: 1 to 80: 1. 80: 1.

In a preferred arrangement, the gas distributor 9 is positioned vertically above the horizontal base element 11 of the baffle 7 and below the top of the peripheral wall 12.

In a preferred arrangement, the gas distributor 9 is a ring type gas distributor. The term ring type gas distributor includes double ring type gas distributors and other multiple ring shapes of ring type gas distributors.

In another particular embodiment, the gas distributor 9 is a ring-type gas distributor, and the radius M of the gas distributor 9 is greater than the radius N of the horizontal base element 11 of the baffle 7 Big and smaller than the radius O of the vertical peripheral wall 12 of the baffle 7.

In another particular embodiment, the gas distributor 9 is a ring-type gas distributor, and the radius M of the gas distributor 9 is greater than the radius N of the horizontal base element 11 of the baffle 7 It is small and smaller than the radius O of the vertical peripheral wall 12 of the baffle 7.

In another particular embodiment, the gas distributor 9 is a ring-type gas distributor, and the ratio of the radius M of the gas distributor 9 to the radius O of the vertical peripheral wall 12 is 0.75: 1 to 0.95: 1.

In a preferred arrangement, the ratio of the height E of the gas distributor 9 over the horizontal base element 11 of the baffle 7 to the radius O of the vertical peripheral wall 12 is from 0.15: 1 to 0.5: 1.

In a preferred arrangement, the horizontal base element 11 of the baffle 7 is located at a first distance H below the lower part of the cylindrical part 1 of the reactor, and the vertical peripheral wall 12 of the baffle 7 ) Is located at a second distance (I) below the lower part of the cylindrical part (1) of the reactor, and the ratio of the first distance (H) to the height (B) of the cylindrical part (1) of the reactor is 0.15: It is in the range of 1 to 0.5: 1, and the ratio of the second distance I to the height B of the cylindrical portion 1 of the reactor is in the range of 0.1: 1 to 0.3: 1.

In a preferred arrangement, the ratio of the diameter G of the liquid nozzle 5 to the diameter D of the cylindrical portion 1 of the reactor ranges from 1: 100 to 1: 5, and the liquid nozzle 5 is a reactor Located at a distance A below the upper portion of the cylindrical portion 1, the ratio of the distance A to the height B of the cylindrical portion 1 of the reactor ranges from 1:10 to 1: 2.5.

In a preferred arrangement, the ratio of the diameter F of the liquid outlet 10 to the diameter D of the cylindrical portion 1 of the reactor ranges from 1:20 to 1: 5.

In a preferred arrangement, the upper enclosure 2 is a hemispherical enclosure extending upwards, and the lower enclosure 3 is a hemispherical enclosure extending downwards.

With this utility model, the downward spray direction of the liquid spray module is the opposite direction of the natural upward direction of gas flow in the liquid reaction medium. Due to the downward flow of the liquid, at least a portion of the gas released from the gas distributor is carried in the flow of the liquid in the baffle, and then the liquid impinging on the baffle is the gas released from the gas distributor in the flow of the liquid (bubbles or Dissolved) is deflected upward. The liquid reaction medium is removed from the reactor through a liquid outlet located at the bottom of the reactor. Due to the arrangement of the downward flow of liquid introduced into the reactor, the position and shape of the baffle, and the position of the liquid outlet, good gas / liquid mixing is achieved across the reactor. When the liquid spray of the above-described liquid spray module is sprayed downward in the vertical direction, the reduced pipe causes an increase in flow velocity; The aforementioned gas distributor is preferably a ring type gas distributor, which has uniformly spaced vents at equal distances from each other, which promotes uniform distribution of the gas phase. By combining vapor distribution and liquid spray filling approaches with the effects of baffles, this utility model maximizes the reaction volume and achieves effective gas / liquid mixing in the reactor, solving the unstable problems caused by mechanical mixing. And reduce so-called dead zones in the reactor. The hydrodynamic reactor to which this utility model relates is intended for use in the liquid phase production of acetic acid by carbonylation of methanol and / or its reaction derivatives in the presence of a catalyst system based on rhodium or iridium, and highly productive acetic acid and carbon monoxide To achieve high conversion.

1 is a graphic diagram of a cross section through a side elevation of the reactor of the utility model.
2 is a graphical view of the top elevation of the baffle and gas distributor arrangement.

1 and 2, reference numeral 1 is a cylindrical part of the reactor, reference numeral 2 is an upper enclosure of the reactor, reference numeral 3 is a lower enclosure of the reactor, reference numeral 4 is a liquid inlet, reference numeral 5 is a liquid nozzle, and reference numerals. 6 is gas outlet, 7 is baffle, 8 is gas inlet, 9 is gas distributor, 10 is liquid outlet, 11 is the horizontal base element of the baffle, 12 is baffle (7 ), The peripheral wall of the vertical direction, 13 is the angled peripheral wall of the baffle 7, A is the distance the liquid nozzle 5 is located below the top of the cylindrical part 1, B is the cylindrical part ( The height of 1), reference C is the overall height of the reactor, reference D is the diameter of the cylindrical part 1, reference E is the height of the gas distributor 9 over the horizontal base element 11, reference F Is the diameter of the liquid outlet 10, reference G is liquid The diameter of the nozzle 5, reference H is the first distance down the bottom of the cylindrical part 1 of the reactor, reference I is the second distance down the bottom of the cylindrical part 1 of the reactor, reference J Is the height of the vertical peripheral wall 12, reference K is the first gap between the edge where the vertical peripheral wall 12 and the angled peripheral wall 13 meet and the inner surface of the lower enclosure 3, reference L Is the second gap between the inner surface of the lower enclosure and the edge where the angled peripheral wall 12 and the horizontal base element 13 meet, reference M is the radius of the gas distributor 9, reference N is the horizontal base element The radius of (11), reference numeral O is the radius of the vertical peripheral wall (12).

The reactor related to the utility model includes a reactor including a cylindrical portion 1, an upper enclosure 2 and a lower enclosure 3; A liquid inlet 4 connected to the liquid nozzle 5; Gas outlet 6; A baffle (7) comprising a horizontal base element (11), a vertical peripheral wall (12) and an angled peripheral wall (13); A gas inlet 8 connected to a gas distributor 9; And a liquid outlet (10). During the use of the reactor in the carbonylation process, the reactor is filled with a liquid reaction medium to a level above the outlet of the liquid nozzle 5, typically up to the top of the cylindrical portion 1 of the reactor. A stream liquid reaction medium comprising a liquid reactant, for example methanol and / or a reaction derivative thereof, enters the reactor at a downward flow from the liquid nozzle 5 so that the stream strikes the baffle 7. A gaseous reactant, for example carbon monoxide, enters the reactor through a gas distributor 9 located above the baffle 7. The downstream stream of the liquid reaction medium flows through an area where gaseous reactants are introduced into the reactor and the flow of the stream of liquid reaction medium picks up at least a portion of the gaseous reactant from this flow, after which the stream is baffle (7) Crashes on. The stream of liquid reaction medium impinging on the baffle 7 is thus transverse to the horizontal base element 11 of the baffle 7 and to the angle of the angled peripheral wall 13 of the baffle 7 and the vertical peripheral wall ( Deflected upward through 12) to form substantial back mixing and increase residence time of gaseous reactants in the liquid reaction medium. The liquid and gas are mixed and circulated over the reactor portion above the baffle 7 due to the aforementioned downward flow of the liquid reaction medium impinging on the baffle 7. The reaction product, for example a liquid reaction medium comprising products of the carbonylation reaction, is withdrawn from the reactor through a liquid outlet 10 located at the bottom of the reactor. Continuous withdrawal of the liquid reaction medium through the liquid outlet 10 located under the baffle 7 maintains a constant liquid level at the top of the cylindrical portion 1 of the reactor through level control, and the liquid nozzle 5 Is maintained by immersion, and forms a circulation of a liquid reaction medium containing gaseous reactants in the reactor. The flow of liquid entering the reactor through the liquid nozzle 5 is ensured to ensure complete mixing over the entire reactor such that there are no dead spots in the reactor where the carbon monoxide reactant is reduced and no reaction occurs and no overmixing occurs. The rate can be adjusted as well as the positions of the baffle 7, gas distributor 9 and liquid nozzle 5. The term " overmixing " refers to the mixing of gas and liquid to the extent that the surface of the liquid reaction medium in the reactor is agitated or stirred extensively. Without time to dissolve, the rate of escape through the surface of the liquid reaction medium is increased. Aeration of gas through the gas outlet 6 can be used to control the pressure in the reactor.

The following implementations provide a more detailed description of this utility model.

Special implementation 1 and implementation 2

Hydrodynamics with all of the features described above and constructed as shown in FIGS. 1 and 2 and having the dimensions as described below in Table 1 in a process for producing acetic acid by carbonylation of carbon monoxide and methanol. Through the use of the reactor, good gas / liquid mixing can be easily achieved without reducing carbon monoxide in the localized volumes of the liquid reaction medium in the reactor, so that the carbon monoxide fed to the reaction and the volume of available reactor It ensures efficient use.

Claims (10)

As a type of hydrodynamic reactor, the hydrodynamic reactor is a vertical cylindrical configuration comprising a cylindrical portion (1), an upper enclosure (2) and a lower enclosure (3), the lower enclosure (3) extending downward A curved enclosure, wherein the hydrodynamic reactor comprises a liquid inlet (4), a liquid nozzle (5), a gas outlet (6), a baffle (7), a gas inlet (8), a gas distributor (9), and a liquid outlet (10) ) Contains:
-The liquid inlet (4) is located at the top of the hydrodynamic reactor, and the distance from the top of the cylindrical portion (1) of the hydrodynamic reactor, or below the top of the cylindrical portion (1) of the hydrodynamic reactor Connected to a liquid nozzle 5 located in the radial center at (A), said liquid nozzle 5 being configured to discharge the liquid in a downward direction;
-The gas outlet (6) is located in the upper enclosure of the hydrodynamic reactor;
-The baffle (7) is located radially centered in the lower enclosure (3) of the hydrodynamic reactor, the baffle (7) is relative to the horizontal base element (11), the horizontal base element (11) A vertical peripheral wall (12) extending upwardly, and an angled peripheral wall (13) connecting the horizontal base element (11) and the vertical peripheral wall (12);
-The gas inlet (8) is located at the bottom of the hydrodynamic reactor and connected to the gas distributor (9);
-The gas distributor 9 is: radially centered within the diameter described by the vertical peripheral wall 12 of the baffle 7 and not lower than the horizontal base element 11 and also vertically Direction is located vertically at a position not higher than the top of the peripheral wall 12; Or in a diameter drawn by the vertical peripheral wall 12 of the baffle 7 and located vertically in the radial center and above the vertical peripheral wall 12 and the gas distributor 9 is connected to the baffle ( 7) configured to expel gas towards the volume defined within;
-The liquid outlet (10) is located in the radial center at the bottom of the lower enclosure (3) of the hydrodynamic reactor;
The ratio of the diameter (D) of the cylindrical portion (1) of the hydrodynamic reactor to the height (B) of the cylindrical portion (1) of the hydrodynamic reactor is in the range of 1.5: 1 to 1: 3, and the fluid The ratio of the height B of the cylindrical portion 1 of the hydrodynamic reactor to the total height C of the dynamics reactor ranges from 1: 1 to 1: 3;
The ratio of the radius N of the horizontal base element 11 of the baffle 7 to the radius 0 of the vertical peripheral wall 12 of the baffle 7 is from 0.3: 1 to 0.95: 1. Range, and the ratio of the height J of the vertical peripheral wall 12 of the baffle 7 to the radius 0 of the vertical peripheral wall 12 of the baffle 7 is 1:15 to 1: In the range of 5;
-The baffle (7) is such that a first gap (K) is provided between the edge where the vertical peripheral wall (12) and the angled peripheral wall (13) meet and the inner surface of the lower enclosure (3); and The second gap (L) is positioned between the angled peripheral wall (13) and the edge where the horizontal base element (11) meets and the inner surface of the lower enclosure (3), and the first gap (K) The ratio of the diameter D of the cylindrical portion 1 of the hydrodynamic reactor to the distance ranges from 10: 1 to 60: 1, and the cylindrical portion of the hydrodynamic reactor to the distance of the second gap L The ratio of diameter (D) of (1) is in the range of 10: 1 to 80: 1, hydrodynamic reactor. According to claim 1,
The gas distributor (9) is positioned vertically above the horizontal base element (11) of the baffle (7) and below the top of the peripheral wall (12). According to claim 1,
The gas distributor 9 is a ring type gas distributor, a hydrodynamic reactor. The method of claim 3,
The hydrodynamic reactor, wherein the radius (M) of the gas distributor (9) is smaller than the radius (O) of the vertical peripheral wall (12) of the baffle (7). The method of claim 3,
The ratio of the radius (M) of the gas distributor (9) to the radius (O) of the vertical peripheral wall (12) ranges from 0.75: 1 to 0.95: 1, hydrodynamic reactor. The method according to any one of claims 1 to 5,
The ratio of the height E of the gas distributor 9 on the horizontal base element 11 of the baffle 7 to the radius O of the vertical peripheral wall 12 is 0.15: 1 to 0.5: Hydrodynamic reactor, in the range of 1. The method according to any one of claims 1 to 5,
The horizontal base element 11 of the baffle 7 is located at a first distance H below the lower portion of the cylindrical part 1 of the hydrodynamic reactor, the vertical peripheral wall of the baffle 7 The upper part of (12) is located at a second distance (I) below the lower part of the cylindrical part (1) of the hydrodynamic reactor, the first with respect to the height (B) of the cylindrical part (1) of the hydrodynamic reactor The ratio of the distance H is in the range of 0.15: 1 to 0.5: 1, and the ratio of the second distance I to the height B of the cylindrical portion 1 of the hydrodynamic reactor is 0.1: 1 to 0.3 Hydrodynamic reactor in the: 1 range. The method according to any one of claims 1 to 5,
The ratio of the diameter G of the liquid nozzle 5 to the diameter D of the cylindrical portion 1 of the hydrodynamic reactor ranges from 1: 100 to 1: 5, and the liquid nozzle 5 is the The ratio of the distance (A) to the height (B) of the cylindrical portion (1) of the hydrodynamic reactor is located at a distance (A) above and below the upper portion of the hydrodynamic reactor (1) to 1 Hydrodynamic reactor, in the range of: 2.5. The method according to any one of claims 1 to 5,
The ratio of the diameter (F) of the liquid outlet (10) to the diameter (D) of the cylindrical portion (1) of the hydrodynamic reactor is in the range of 1:20 to 1: 5, hydrodynamic reactor. The method according to any one of claims 1 to 5,
The upper enclosure 2 is a hemispherical enclosure extending upwards, and the lower enclosure 3 is a hemispherical enclosure extending downwards, a hydrodynamic reactor.

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