TW202028168A - Production apparatus of methacrylic acid - Google Patents

Abstract

The invention provides a production apparatus of methacrylic acid. The production apparatus can simplify equipment. The production apparatus comprises a first reactor (10); second reactors (R1 to Rn)n represent an integer greater than 2; pipelines (LA) for connecting the outlet of the first reactor (10) with the inlets of the second reactors (R1 to Rn) and providing the material flow branches from the outlet of the first reactor (10) to the inlets of the second reactors (R1 to Rn); and pipelines (LB), which are connected to the outlets of the second reactors (R1 to Rn) and merge the materialflows from the outlets of the second reactors (R1 to Rn). The heights (A) of the bottoms of the second reactors (R1 to Rn), the heights (H) of the second reactors (R1 to Rn), the pipelines in the runners from the branches of the pipelines (LA) to the second reactors (R1 to Rn), and the pipelines in the runners from the outlets of the second reactors (R1 to Rn) to the converging part of the pipelines (LB) all meet required conditions.

Description

Manufacturing equipment for methacrylic acid

The present invention relates to a manufacturing device of methacrylic acid.

Patent Document 1 describes a method for producing methacrylic acid. [Prior Technical Literature] [Patent Literature]

[Patent Document 1] International Publication No. 2008/145417

[The problem to be solved by the invention]

The manufacturing device for manufacturing methacrylic acid is preferably simple in equipment. Therefore, the object of the present invention is to provide a methacrylic acid manufacturing device that can simplify equipment. [Technical means to solve the problem]

The methacrylic acid production apparatus of the present invention includes: a first reactor for obtaining methacrolein from isobutylene and/or tertiary butanol (hereinafter referred to as "TBA") and oxygen; and a plurality of second reactors R ₁ ~R _n (n represents an integer of 2 or more), which reacts methacrolein and oxygen to obtain methacrylic acid; line LA is connected to the outlet of the first reactor and the second reactor R ₁ to R _n The inlet, which branches the stream flowing out from the outlet of the first reactor and supplies it to the respective inlets of the second reactors R ₁ to R _n ; and a line LB, which is connected to the respective outlets of the second reactors R ₁ to R _n the second from the reactor R ₁ ~ R _n ilk outlet to the junction, and the second reactor R ₁ ~ R _n of the height of the bottom of each of A ₁ ~ A _n satisfies the formula (2) of the second embodiment is provided The heights H ₁ ～H _{n of the} reactors R ₁ ～R _n and the second reactors R ₁ ～R _n satisfy the formula (3), from the branch of the pipeline LA to the inlet R of the second reactor R ₁ ～R _{n 1i} ~ a flow path of the respective _ni R C1i ~ pipe inner diameter D of the upper and Cni _1i ~ D _ni length L _1i ~ L _ni satisfies the following formula (4a) and formula (4b) of the condition, from the second reactors R ₁ to ~ R _n of outlet R _1j ~ merging portion R _nj to line LB of each of a flow path of C1j ~ inner diameter D of the pipe of the sum Cnj _1j ~ D _nj and a length L _1j ~ L _nj satisfy the formula (5a) and ( The conditions of 5b). (A _max －A _min )/A _ave ≦0.02 …(2) [A _max represents the maximum value of A ₁ ～A _n , A _min represents the minimum value of A ₁ ～A _n , A _ave represents A ₁ ～A Average value of _n ] (H _max －H _min )/H _ave ≦0.02 …(3) [H _max represents the maximum value of H ₁ ～H _n , H _min represents the minimum value of H ₁ ～H _n , H _ave Represents the average value of H ₁ ～H _n ] (D _max(i) /D _min(i) )≦1.025 …(4a) [D _max(i) represents the maximum value of D _1i ～D _ni , D _{min(i )} Represents the minimum value of D _1i ～D _ni ] (L _max(i) /L _min(i) )≦1.05 …(4b) [L _max(i) represents the maximum value of L _1i ～L _ni , L _{min (i)} represents the minimum value of L _1i ～L _ni ] (D _max(j) /D _min(j) )≦1.025 …(5a) [D _max(j) represents the maximum value of D _1j ～D _nj , D _min(j) represents the minimum value of D _1j ～D _nj ] (L _max(j) /L _min(j) )≦1.05 …(5b) [L _max(j) represents the maximum value of L _1j ～L _nj Value, L _min(j) represents the minimum value among L _1j ～L _nj ]

According to this methacrylic acid manufacturing device, the equipment can be simplified.

In the above-mentioned methacrylic acid production apparatus, it is preferable that when the same fluid is passed through the flow paths C1i to Cni at the same flow rate, the pressure loss ΔP _1i to ΔP _ni between the inlet and the outlet of each flow path C1i to Cni satisfies Equation (1a), when the same fluid is passed through the flow paths C1j to Cnj at the same flow rate, the pressure loss ΔP _1j to ΔP _nj between the inlet and the outlet of each flow path C1j to Cnj satisfy the equation (1b). (ΔP _max(i) －ΔP _min(i) )/ΔP _ave(i) ≦0.10 …(1a) [ΔP _max(i) represents the maximum value among ΔP _1i ～ΔP _ni , and ΔP _min(i) represents ΔP _1i ～The minimum value of ΔP _ni , ΔP _ave(i) represents the average value of ΔP _1i ～ΔP _ni ] (ΔP _max(j) －ΔP _min(j) )/ΔP _ave(j) ≦0.10 …(1b) [ΔP _max(j) represents the maximum value of ΔP _1j ～ΔP _nj , ΔP _min(j) represents the minimum value of ΔP _1j ～ΔP _nj , and ΔP _ave(j) represents the average value of ΔP _1j ～ΔP _nj ]

In this way, the equipment can be further simplified. [Effects of Invention]

According to the present invention, a methacrylic acid manufacturing device that can simplify equipment is provided.

In this specification, the so-called isobutylene refers to 2-methylpropene.

First, referring to FIG. 1, the methacrylic acid production apparatus 100 of this embodiment will be described. Fig. 1 is a diagram showing an example of a methacrylic acid production apparatus of the present embodiment.

The manufacturing device 100 is an example of a manufacturing device when the second reactor includes two reactors. That is, the manufacturing apparatus 100 shows an aspect when n is 2 in a plurality of second reactors R ₁ to R _n (n represents an integer of 2 or more). In the description of the manufacturing apparatus 100, "A ₁ ～A _n ", "H ₁ ～H _n ", "D _1i ～D _ni ", "L _1i ～L _ni ", "D _1j ～D _nj ", "L _1j ～L _nj ”, “ΔP _1i ～ΔP _ni ”and “ΔP _1j ～ΔP _nj ” respectively mean “A ₁ and A ₂ ”, “H ₁ and H ₂ ”, “D _1i and D _2i ”, "L _1i and L _2i ", "D _1j and D _2j ", "L _1j and L _2j ", "ΔP _1i and ΔP _2i ", and "ΔP _1j and ΔP _2j ".

The manufacturing apparatus 100 mainly includes a first reactor 10, a second reactor 20, a separation mechanism 60, and lines LA and LB. The line LA is equipped with a gas mixer 50b. The second reactor 20 includes reactors R ₁ and R ₂ .

The inlet 10i of the first reactor 10 is connected via a line L10 to a supply source (S0) of a gas containing isobutylene and/or TBA and oxygen.

The first reactor 10 is a reactor for obtaining methacrolein from isobutylene and/or TBA and oxygen.

The first reactor 10 is preferably a reactor filled with a catalyst in a container. The first reactor 10 may be a fixed bed reactor filled with a catalyst in the container. There is no restriction on the direction of flow, and it can be an upward flow or a downward flow. Examples of catalysts used in the synthesis of methacrolein from isobutylene and/or TBA and oxygen are metal oxides containing molybdenum and bismuth.

In the case of obtaining methacrolein from isobutylene and oxygen, isobutylene reacts with oxygen, thereby generating methacrolein. TBA can also be used instead of isobutylene. It is thought that when methacrolein is obtained from TBA and oxygen, isobutene is produced by the dehydration reaction of TBA, and the produced isobutene reacts with oxygen to produce methacrolein. It is believed that the reason why TBA can be used instead of isobutylene is that in the first reactor 10, the oxidation reaction of isobutylene becomes a rate limit. Isobutylene and TBA can also be used together.

The outlet 10j of the first reactor 10 and the inlets R _1i and R _{2i of the} second reactor 20 are connected by a line LA. The inlets R _1i and R _{2i of the} second reactor 20 are the inlets of the reactors R ₁ and R ₂ respectively. The line LA is a line that branches the stream flowing out of the outlet 10j of the first reactor 10 and supplies it to the respective inlets of the reactors R ₁ and R ₂ .

A line L22 is connected to the inlet 50b _m of the gas mixer 50b of the line LA. The pipeline L22 is a pipeline connecting the pipeline LA and the oxygen supply source (S1), and a compressor 55 is provided in a part of the pipeline.

The second reactor 20 is a reactor for obtaining methacrylic acid by reacting methacrolein and oxygen. The reactor constituting the second reactor 20 is preferably a reactor filled with a catalyst in the container. The reactor constituting the second reactor 20 may be a fixed bed reactor filled with a catalyst in the container. The fixed-bed reaction device may also be, for example, a device formed by filling solid particles including catalyst particles and optionally inert particles into each tube body of a multi-tube heat exchanger. The flow direction of the flow is not particularly limited, and it may be an upward flow or a downward flow. An example of the catalyst used in the reaction of synthesizing methacrylic acid from methacrolein and oxygen is a heteropolyacid compound containing phosphorus and molybdenum.

The outlets R _1j and R _{2j of the} second reactor 20 and the inlet 60i of the separation mechanism 60 are connected by a pipeline LB. The outlets R _1j and R _{2j of the} second reactor 20 are the outlets of the reactors R ₁ and R ₂ respectively. The pipeline LB is a pipeline that merges the streams flowing out of the outlets of the reactors R ₁ and R ₂ and supplies them to the separation mechanism 60.

The reactors R ₁ and R ₂ are set up in such a way that the heights A ₁ and A _{2 of the} respective bottoms satisfy the formula (2). The reactor R ₁ and R ₂ are each of a height H ₁ and H ₂ satisfies the formula (3). Here, height means the length in the vertical direction. The height A of the bottom of the reactor means the height from the ground surface to the bottom of the reactor, and the height H of the reactor means the height of the reactor itself. (A _max －A _min )/A _ave ≦0.02 …(2) [A _max represents the maximum value of A ₁ ～A _n , A _min represents the minimum value of A ₁ ～A _n , A _ave represents A ₁ ～A Average value of _n ] (H _max －H _min )/H _ave ≦0.02 …(3) [H _max represents the maximum value of H ₁ ～H _n , H _min represents the minimum value of H ₁ ～H _n , H _ave Represents the average value of H ₁ ～H _n ]

A _ave may be, for example, 1-15 m, 2-12 m, or 4-10 m.

H _ave may be, for example, 1 to 12 m, 2 to 10 m, or 4 to 8 m.

The inner diameter D _1i and length L _{1i of the} pipe on the flow path C1i from the branch Xa of the pipeline LA to the inlet R _1i of the reactor R ₁ , and the branch Xa of the pipeline LA to the inlet R of the reactor R ₂ until the condition of the pipe inner diameter D _2i on the road C2i ilk _2i and _2i length L satisfies the formula (4a) and formula (4b) of. (D _max(i) /D _min(i) )≦1.025 …(4a) [D _max(i) represents the maximum value among D _1i ～D _ni , and D _min(i) represents the minimum value among D _1i ～D _ni Value] (L _max(i) /L _min(i) )≦1.05 …(4b) [L _max(i) represents the maximum value of L _1i ～L _ni , L _min(i) represents L _1i ～L _ni Minimum]

The inner diameter D _1j and the length L _{1j of the} pipe on the flow path C1j from the outlet R _{1j of the} reactor R ₁ to the junction Xb of the pipeline LB, and the junction from the outlet R _{2j of the} reactor R ₂ to the pipeline LB The inner diameter D _2j and the length L _{2j of the} pipe on the flow path C2j up to Xb satisfy the conditions of formulas (5a) and (5b). (D _max(j) /D _min(j) )≦1.025 …(5a) [D _max(j) represents the maximum value of D _1j ～D _nj , D _min(j) represents the minimum value of D _1j ～D _nj Value] (L _max(j) /L _min(j) )≦1.05 …(5b) [L _max(j) represents the maximum value of L _1j ～L _nj , L _min(j) represents L _1j ～L _nj Minimum]

In this specification, the inner diameter of the pipe means the average value of the integral in the length direction of the inner diameter of the pipe. In addition, the length of the pipe means the length of the central axis of the pipe.

D _max(i) may be 200-1800 mm, 400-1500 mm, or 600-1300 mm, for example.

L _max(i) may be, for example, 1 to 40 m, 5 to 35 m, or 10 to 30 m.

D _max(j) may be 200 to 1800 mm, 400 to 1500 mm, or 600 to 1300 mm, for example.

L _max(j) may be, for example, 1 to 40 m, 5 to 35 m, or 10 to 30 m.

Regarding the manufacturing apparatus 100, from the viewpoint of simplifying the equipment further, it is preferable that the pressure loss ΔP _1i and the flow between the inlet and the outlet of the flow path C1i when the same fluid is passed through the flow paths C1i and C2i at the same flow rate The pressure loss ΔP _2i between the inlet and the outlet on the path C2i satisfies the formula (1a). When the same fluid is passed through the flow paths C1j and C2j at the same flow rate, the pressure loss between the inlet and the outlet on the flow path C1j is ΔP _1j And the pressure loss ΔP _2j between the inlet and the outlet on the flow path C2j satisfies the formula (1b). Here, the same fluid means fluids with the same composition, temperature and pressure. (ΔP _max(i) －ΔP _min(i) )/ΔP _ave(i) ≦0.10 …(1a) [ΔP _max(i) represents the maximum value among ΔP _1i ～ΔP _ni , and ΔP _min(i) represents ΔP _1i ～The minimum value of ΔP _ni , ΔP _ave(i) represents the average value of ΔP _1i ～ΔP _ni ] (ΔP _max(j) －ΔP _min(j) )/ΔP _ave(j) ≦0.10 …(1b) [ΔP _max(j) represents the maximum value of ΔP _1j ～ΔP _nj , ΔP _min(j) represents the minimum value of ΔP _1j ～ΔP _nj , and ΔP _ave(j) represents the average value of ΔP _1j ～ΔP _nj ]

The flow path C1i from the branch Xa to the inlet R _1i of the reactor R _{1 and} the flow path C2i from the branch Xa to the inlet R _2i of the reactor R ₂ may be substantially identical in shape. Therefore, there is a tendency that the manufacturing apparatus 100 easily satisfies the range of the formula (1a). An outlet from the reactor R ₁ of R Xb ilk path up to the merging portion _1j C1j, the outlet from the reactor R ₂ of the R Xb ilk passage _2j up to the merging portion C2j shape may be substantially congruent thereto. Thereby, there is a tendency that the manufacturing apparatus 100 easily satisfies the range of the formula (1b). The shape of the pipe contained between the branch part Xa and the confluence part Xb may be approximately symmetrical with respect to any one of the planes including the line connecting the branch part Xa and the confluence part Xb.

The separation mechanism 60 discharges a stream containing carbon monoxide, carbon dioxide, nitrogen, argon, light components and oxygen from the first outlet (F35), and discharges a stream containing methacrylic acid and heavy components (F31) from the second outlet (F31), and from the third outlet The outlet discharges a stream containing methacrolein (F23). A pipeline L35 is connected to the first outlet, a pipeline L31 is connected to the second outlet, and a pipeline L23 is connected to the third outlet.

The pipeline L23 is connected to the pipeline LA.

Examples of the separation mechanism 60 include distillation towers, extraction towers, absorption towers, and combinations of these. When the separation mechanism 60 includes one distillation column, it is preferable to install the line L35 at the upper part of the distillation column, install the line L31 at the lower part of the distillation column, and install the line L23 at the side of the distillation column.

Next, the manufacturing method of methacrylic acid of this embodiment is demonstrated.

(Supply source) Prepare a stream (F10) containing isobutene and/or TBA and oxygen as a supply source (S0) of gas containing isobutene and/or TBA and oxygen.

The stream (F10) may also contain components other than isobutylene, TBA, and oxygen. Examples of components other than isobutene, TBA and oxygen include C5 olefins such as isoprene, isobutane, 1-butene, 2-butene (cis, trans), propane, propylene, n-butane Alkane, methyl tert-butyl ether, methanol, dimethyl ether, butadiene, propadiene, diisobutene, nitrogen, carbon dioxide, carbon monoxide, water and argon.

The concentration of isobutylene and/or TBA in the stream (F10) is calculated based on the total concentration of isobutylene and TBA, for example, 1% by mass or more, 2% by mass or more, or 4% by mass or more. The total concentration of isobutylene and TBA in the stream (F10) is, for example, 21% by mass or less, 19% by mass or less, or 17% by mass or less. The total concentration of isobutylene and TBA in the stream (F10) is preferably from 1 to 21% by mass, more preferably from 2 to 19% by mass, and still more preferably from 4 to 17% by mass.

The oxygen concentration in the flow (F10) is, for example, 7 mass% or more, 8 mass% or more, or 10 mass% or more. The oxygen concentration in the flow (F10) is, for example, 24% by mass or less, 23% by mass or less, or 21% by mass or less. The oxygen concentration in the stream (F10) is preferably 7 to 24% by mass, more preferably 8 to 23% by mass, and still more preferably 10 to 21% by mass.

In addition, a stream (F22) containing oxygen as an oxygen supply source (S1) is prepared.

The concentration of oxygen in the flow (F22) is, for example, 15% by mass or more. The concentration of oxygen in the stream (F22) is preferably 16% by mass or more, more preferably 17% by mass or more, and still more preferably 20% by mass or more. The upper limit of the oxygen concentration in the flow (F22) can be set to, for example, 35% by mass. The concentration of oxygen in the flow (F22) may be 30% by mass or less, or 25% by mass or less, for example. The oxygen concentration in the stream (F22) is preferably 16 to 35% by mass, more preferably 17 to 30% by mass, and still more preferably 18 to 25% by mass.

(Reaction step) The stream (F10) is supplied to the first reactor 10, and in the first reactor 10, isobutene and oxygen in the stream (F10) are reacted. The stream (F11) containing methacrolein obtained by the reaction of isobutylene and oxygen is discharged from the line LA.

The reaction temperature of the first reactor 10 can be set at 300-400°C. The reaction pressure of the first reactor 10 can be set to 0.004 to 0.6 MPaG (gauge pressure).

In the stream (F11) discharged from the first reactor 10, the stream (F23) containing methacrolein is mixed through the line L23, and the stream (F22) containing oxygen is mixed through the line L22. Thereby, the obtained stream (F21) is supplied to each reactor (R ₁ and R ₂ ) of the second reactor 20 via the line LA.

The concentration of methacrolein in the stream (F23) is preferably 0.1% by mass or more, more preferably 3% by mass or more, and still more preferably 7% by mass or more. The concentration of methacrolein in (F23) is preferably 32% by mass or less, more preferably 23% by mass or less, and still more preferably 16% by mass or less. The concentration of methacrolein in the stream (F23) can be 0.1 to 32% by mass, 3 to 23% by mass, or 7 to 16% by mass. The stream (F23) may contain nitrogen, water, and carbon dioxide as components other than methacrolein, for example.

In the second reactor 20, methacrolein and oxygen are reacted to obtain methacrylic acid, and a stream containing methacrylic acid is discharged through line LB (F30).

Stream (F30) usually contains unreacted methacrolein. The stream (F30) may contain components other than methacrylic acid and methacrolein. Examples of such components include acrylic acid, acrolein, nitrogen, argon, oxygen, water, carbon monoxide, carbon dioxide, acetaldehyde, propionaldehyde, terephthalic acid, maleic acid, fumaric acid, diacetin, isobenzene Dicarboxylic acid, isobutyric acid, methyl furfural, acetic acid, propionic acid, etc.

The reaction temperature of the second reactor 20 can be set at 200-350°C. The reaction pressure in the second reactor 20 is, for example, 0.01 to 0.3 MPaG.

(Separation step and recovery step) The stream (F30) is supplied to the separation mechanism 60 via the line LB. The stream is separated in the separation mechanism 60, the stream containing carbon monoxide, carbon dioxide, nitrogen, argon, light components and oxygen is extracted from the line L35 (F35), and the stream containing methacrylic acid and heavy components is extracted from the line L31 (F31 ), and withdraw the stream (F23) containing methacrolein from the line L23.

The stream (F23) containing methacrolein is merged to the stream (F11) via the line L23.

The methacrylic acid production device 100 includes: a first reactor 10 that obtains methacrolein from isobutylene and/or TBA and oxygen; and a plurality of second reactors 20 (R ₁ and R ₂ ) that make methacrylic acid Aldehydes and oxygen react to obtain methacrylic acid; line LA, which is connected to the outlet 10j of the first reactor 10 and the inlet of the second reactor 20 (R ₁ and R ₂ ), will be from the outlet 10j of the first reactor 10 The outflowing stream is branched and supplied to each inlet of the second reactor 20 (R ₁ and R ₂ ); and a line LB, which is connected to each outlet of the second reactor 20 (R ₁ and R ₂ ), so that 20 is for the two reactors (R ₁ and R ₂₎ flows out of the outlet merging ilk, and as to the height of the bottom of each reactor A is R ₁ and R _{2 1} and A ₂ satisfy the formula (2) of the set, reactors R ₁ to The heights H ₁ and H _{2 of} R ₂ and R ₂ satisfy the formula (3), and the piping on the respective flow paths C1i and C2i from the branch Xa of the pipeline LA to the inlets R _1i and R _2i of the reactors R ₁ and R ₂ The inner diameters D _1i and D _2i and the lengths L _1i and L _2i satisfy the conditions of formula (4a) and formula (4b), from the outlets R _1j and R _{2j of the} reactors R ₁ and R ₂ to the junction Xb of the pipeline LB The inner diameters D _1j and D _2j and the lengths L _1j and L _{2j of the} pipes on the respective flow paths C1j and C2j so far satisfy the conditions of equations (5a) and (5b). From this, it is considered that even if a valve or the like is not provided in the line LA, it is easy to make the fluid flow evenly through the reactors R ₁ and R ₂ , so that the equipment can be simplified, and the long-term stable operation can be achieved without particularly complicated operations. It is also believed that because it is not necessary to install a valve or the like at the above-mentioned position, it is also possible to prevent the clogging of the pipe at the complicated shape such as the valve. In addition, since the methacrylic acid production apparatus 100 has a plurality of second reactors, it tends to be easier to fill the second reactor with more catalyst than the required amount. It is believed that by filling the amount of catalyst in the second reactor more than required, for example, even when the catalyst activity of the second reactor is lower than that of the first reactor, it is easy to maintain The productivity of the second reactor.

Since the device of this embodiment is excellent in continuous operation, it is considered that the raw materials and energy during long-term operation can be reduced.

The present invention is not limited to the above-mentioned embodiments, and can be variously modified.

For example, separation and purification mechanisms such as distillation towers and extraction towers may be added to each pipeline.

The gas mixer 50b may be omitted. In this case, the pipeline L22 can be directly connected to the piping of the pipeline L21.

The pipeline L23 is optional. In the methacrylic acid manufacturing device 100, the pipeline L23 is connected to the separation mechanism 60, but the pipeline L23 may not be connected to the separation mechanism 60. That is, the stream supplied to the line LA via the line L23 may not be the stream recovered from the separation mechanism 60.

The second reactor may also include more than 3 reactors. That is, in a plurality of second reactors R ₁ to R _n , n may be 3 or more. In this case, the branch portion of the pipeline LA branches into n flow paths, and the junction portion of the pipeline LB merges with n flow paths. In addition, the reactors R ₁ to R _n can be set as the following devices, that is, the heights A ₁ to A _{n of the} bottoms of the respective bottoms satisfy the formula (2), and the heights H ₁ to H _n satisfy the formula (3) , The inner diameters D _1i to D _ni and lengths L _1i to L _{ni of the} pipes on the respective flow paths C1i to Cni from the branch of the pipeline LA to the inlets R _1i to R _ni of the reactor R ₁ to R _n satisfy the formula The conditions of (4a) and formula (4b) are the inner diameters D _1j to D of the piping on the respective flow paths C1j to Cnj from the exit R _1j to R _{nj of the} reactor R ₁ to R _n to the junction of the pipeline LB _nj and lengths L _1j to L _nj satisfy the conditions of equations (5a) and (5b).

Moreover, when n is 3 or more, it is also preferable to pass the same fluid through the flow paths C1i to Cni at the same flow rate, and the pressure loss ΔP _1i to ΔP between the inlet and the outlet of each flow path C1i to Cni _ni satisfies the formula (1a), and when the same fluid passes through the flow paths C1j to Cnj at the same flow rate, the pressure loss ΔP _1j to ΔP _nj between the inlet and the outlet of the flow paths C1j to Cnj satisfy the formula (1b).

10: First reactor 10i: Inlet 10j: Outlet 20: Second reactor 50b: Gas mixer 50b _m : Inlet 55: Compressor 60: Separation mechanism 60i: Inlet 100: Methacrylic acid manufacturing device C1i: Flow path C1j: Flow path C2i: Flow path C2j: Flow path F10: Flow F11: Flow F21: Flow F22: Flow F23: Flow F30: Flow F31: Flow F35: Flow L10: Pipeline L22: Pipeline L23: Pipeline L31: Pipeline L35: Line LA: Line LB: Line R ₁ : Second Reactor R ₂ : Second Reactor R _1i : Inlet R _1j : Outlet R _2i : Inlet R _2j : Outlet S0: Gas Supply Source S1: Oxygen Supply Source Xa: Branch Xb: Confluence

Fig. 1 is a diagram showing an example of a methacrylic acid production apparatus of the present embodiment.

10: The first reactor

10i: entrance

10j: export

20: second reactor

50b: Gas mixer

50b _m : entrance

55: Compressor

60: Separation mechanism

60i: entrance

100: Manufacturing equipment for methacrylic acid

C1i: flow path

C1j: flow path

C2i: flow path

C2j: flow path

F10: Stream

F11: Stream

F21: Stream

F22: Stream

F23: Stream

F30: flow

F31: Stream

F35: Stream

L10: pipeline

L22: pipeline

L23: pipeline

L31: pipeline

L35: pipeline

LA: pipeline

LB: pipeline

R ₁ : second reactor

R ₂ : Second reactor

R _1i : entrance

R _1j : exit

R _2i : entrance

R _2j : exit

S0: gas supply source

S1: oxygen supply source

Xa: Branch

Xb: Confluence Department

Claims (2)

A manufacturing device for methacrylic acid, comprising: a first reactor for obtaining methacrolein from isobutylene and/or tertiary butanol and oxygen; and a plurality of second reactors R ₁ to R _n (n represents 2 or more Integer), which reacts methacrolein and oxygen to obtain methacrylic acid; Line LA, which is connected to the outlet of the first reactor and the inlet of the second reactor R ₁ ～R _n , will flow from the first reactor The stream flowing out of the outlet of the second reactor is branched and supplied to the respective inlets of the second reactor R ₁ to R _n ; and the pipeline LB, which is connected to the respective outlets of the second reactor R ₁ to R _n , from the second reactor R ₁ ~ R _n ilk outlet to the junction, and the second reactor R ₁ ~ R _n of the height of the bottom of each of A ₁ ~ A _n satisfies the formula (2) of the second reactor disposed R ₁ ~ R _n, The heights H ₁ ～H _{n of the} second reactors R ₁ ～R _n satisfy the formula (3), and each flow from the branch of the pipeline LA to the inlets R _1i ～R _ni of the second reactors R ₁ ～R _n The inner diameters D _1i ～D _ni and lengths L _1i ～L _{ni of the} pipes on paths C1i～Cni satisfy the conditions of formula (4a) and formula (4b), from the exit R _1j ～ of the second reactor R ₁ ～R _n The inner diameter D _1j ～D _nj and the length L _1j ～L _{nj of the} pipes on the respective flow paths C1j～Cnj from R _nj to the confluence part of the pipeline LB satisfy the conditions of formula (5a) and formula (5b), (A _max －A _min )/A _ave ≦0.02 …(2) [A _max represents the maximum value of A ₁ ～A _n , A _min represents the minimum value of A ₁ ～A _n , and A _ave represents the average of A ₁ ～A _n Value] (H _max －H _min )/H _ave ≦0.02 …(3) [H _max represents the maximum value of H ₁ ～H _n , H _min represents the minimum value of H ₁ ～H _n , H _ave represents H ₁ ～H _n average value] (D _max(i) /D _min(i) )≦1.025 …(4a) [D _max(i) represents the maximum value among D _1i ～D _ni , D _min(i) represents D The minimum value of _1i ～D _ni ] (L _max(i) /L _min(i) )≦1.05 …(4b) [L _max(i) represents the maximum value of L _1i ～L _ni , L _min(i) Represents the minimum value of L _1i ～L _ni ] (D _max(j) /D _min(j) )≦1.025 …(5a) [D _max(j) represents the maximum value of D _1j ～D _nj , D _{min( j)} represents the minimum value among D _1j ～D _nj ] (L _max(j) /L _{min (j)} )≦1.05 …(5b) [L _max(j) represents the maximum value of L _1j ～L _nj , L _min(j) represents the minimum value of L _1j ～L _nj ]. Such as the methacrylic acid manufacturing device of claim 1, wherein when the same fluid is passed through the flow paths C1i to Cni at the same flow rate, the pressure loss ΔP _1i to ΔP _ni between the inlet and the outlet of each flow path C1i to Cni satisfies Equation (1a), when the same fluid passes through the flow paths C1j～Cnj at the same flow rate, the pressure loss ΔP _1j ～ΔP _nj between the inlet and the outlet of each flow path C1j～Cnj satisfies the formula (1b), (ΔP _{max (i)} －ΔP _min(i) )/ΔP _ave(i) ≦0.10 …(1a) [ΔP _max(i) represents the maximum value of ΔP _1i ～ΔP _ni , ΔP _min(i) represents ΔP _1i ～ΔP _ni ΔP _ave(i) represents the average value of ΔP _1i ～ΔP _ni ] (ΔP _max(j) －ΔP _min(j) )/ΔP _ave(j) ≦0.10 …(1b) [ΔP _{max(j) )} Represents the maximum value of ΔP _1j ～ΔP _nj , ΔP _min(j) represents the minimum value of ΔP _1j ～ΔP _nj , and ΔP _ave(j) represents the average value of ΔP _1j ～ΔP _nj ].

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