Method and device for strengthening gas phase uniform distribution in gas-liquid mass transfer process

Abstract

The invention provides a gas phase uniform distribution method for strengthening a gas-liquid mass transfer process. The invention further provides a gas phase uniform distribution device for strengthening the gas-liquid mass transfer process. The invention further provides application of the gas phase uniform distribution method for strengthening the gas-liquid mass transfer process or the gas phase uniform distribution device for strengthening the gas-liquid mass transfer process in strengthening the gas-liquid mass transfer process in the bubbling reactor. The invention further provides a bubbling reactor which comprises the gas phase uniform distribution device for strengthening the gas-liquid mass transfer process. According to the method and the device for enhancing gas phase uniform distribution in the gas-liquid mass transfer process, gas-liquid distribution is improved and optimized, the gas-liquid mass transfer coefficient is increased, the gas-liquid mass transfer process is enhanced, and a favorable contact place is provided for gas-liquid two-phase reaction in a reactor.

Description

Technical Field

[0001] The present invention belongs to the field of chemical industry, and relates to a method and device for enhancing the uniform distribution of gas phase in a gas-liquid mass transfer process, and specifically to a gas phase uniform distribution device applied to a gas-liquid two-phase or gas-liquid-solid three-phase system, and its application and a method for enhancing the gas-liquid mass transfer process. Background Art

[0002] In industrial / agricultural design, fluids including but not limited to liquids, gases, gas / liquids or single-phase / multiphase flows are usually evenly distributed first and then evenly merged. Academically, this process of flow division and confluence is called a branch flow process. Common industrial / agricultural processes include irrigation, heating and ventilation, boiler headers, radial reactors, fluidized bed distributors, microreactors, fuel cells, etc. The efficiency of these devices often depends on the uniformity of fluid distribution and pressure drop.

[0003] Gas-liquid bubbling reactor is an important type of equipment that provides gas-liquid contact and reaction, and is widely used in olefin hydroformylation, carbonyl synthesis, oxidative esterification, etc. in the chemical industry. Among them, the gas porous distribution pipe or gas distributor of the bubbling reactor is an important chemical equipment. Its design is very important. It determines the distribution of liquid, gas, gas / liquid or single-phase / multi-phase flow in the reactor, and restricts the mass transfer, heat transfer, transmission and reaction process in the bubbling reactor. The structural design of the gas porous distribution pipe or gas distributor and the distribution performance and the multi-phase distribution in the reactor and the multi-phase structure-activity relationship in the reactor are difficult points. Summary of the invention

[0004] In view of the characteristics of the prior art described above, the purpose of the present invention is to provide a method and device for uniform distribution of the gas phase in order to enhance the gas-liquid mass transfer process. In view of the complex fluid mechanics and strong nonlinear characteristics of the gas-liquid multiphase bubbling reactor in the eccentric jet bubbling reactor, based on the conservation of momentum and mass of the fluid, the liquid, gas, gas / liquid or single-phase / multiphase flow are uniformly distributed, thereby enhancing the gas-liquid mass transfer process and providing a favorable reaction site for the chemical reaction in the bubbling reactor.

[0005] To achieve the above-mentioned object and other related objects, the present invention provides a method for uniformly distributing the gas phase in a gas-liquid mass transfer process in a first aspect, comprising the following steps:

[0006] 1) Take the distribution pipe and set the number of outflow orifices on the pipe wall according to formula (1).

[0007] The formula (1) is:

[0008] In the formula,

[0009] η is the porosity of the distribution pipe, unit is dimensionless;

[0010] n is the number of outflow orifices, pieces;

[0011] d is the diameter of the outflow orifice, mm;

[0012] D is the inner diameter of the distribution pipe, mm;

[0013] L is the length of the distribution pipe, mm;

[0014] 2) With respect to step 1), a distribution pipeline having an outflow orifice is obtained, and the Euler number Eu is calculated according to formula (2) to determine the gas phase uniformity of the distribution pipeline in step 1).

[0015] The formula (2) is:

[0016] In the formula,

[0017] Eu is the Euler number, and its unit is dimensionless;

[0018] X is the dimensionless number of length, and its unit is dimensionless;

[0019] v0 is the flow velocity at the outlet of the distribution pipe, in m / s;

[0020] g is the gravitational acceleration of the fluid, in m / s 2 ;

[0021] L is the length of the distribution pipe, mm;

[0022] E is the aspect ratio, dimensionless;

[0023] Re0 is the outlet Reynolds number of the distribution pipe, unit is dimensionless;

[0024] z is the characteristic parameter of the velocity distribution inside the distribution pipe of the porous fluid, and the unit is dimensionless;

[0025] α is the correction coefficient, specifically the momentum change rate of the fluid flowing through the first hole, or the momentum exchange coefficient of the first hole, which is 0.65;

[0026] β is the correction coefficient, which is the ratio of the porosity η and the aspect ratio E of the porous tube, β≈0.15;

[0027] 3) According to the Euler number Eu obtained in step 2), the pressure difference of the distribution pipeline is determined according to formula (3) to enhance the gas-liquid mass transfer process.

[0028] The formula (2) is:

[0029] In the formula,

[0030] Eu is the Euler number, and its unit is dimensionless;

[0031] P x is the pressure at x, in kPa;

[0032] P0 is the starting point pressure, in kPa;

[0033] ρ is the kinetic energy in the distribution pipe and the density of the medium flowing through it, in kg / m 3 ;

[0034] v0 is the flow velocity of the distribution pipe through the outlet orifice, in m / s.

[0035] The second aspect of the present invention provides a gas phase uniform distribution device for enhancing the gas-liquid mass transfer process, including a distribution pipe with at least one outflow orifice. The distribution pipe with the outflow orifice complies with the above-mentioned gas phase uniform distribution method.

[0036] The third aspect of the present invention provides the above-mentioned gas phase uniform distribution method for enhancing the gas-liquid mass transfer process, or the use of the above-mentioned gas phase uniform distribution device for enhancing the gas-liquid mass transfer process in enhancing the gas-liquid mass transfer process in a bubbling reactor.

[0037] A fourth aspect of the present invention provides a bubbling reactor comprising the gas phase uniform distribution device for enhancing the gas-liquid mass transfer process.

[0038] As described above, the method and device for enhancing the uniform distribution of the gas phase in the gas-liquid mass transfer process provided by the present invention have the following beneficial effects:

[0039] (1) The present invention provides a method and device for enhancing the uniform distribution of the gas phase in the gas-liquid mass transfer process, which optimizes the gas-liquid distribution, improves the gas-liquid mass transfer coefficient, enhances the gas-liquid mass transfer process, and provides a favorable reaction site for the chemical reaction in the reactor.

[0040] (2) The present invention provides a method and device for enhancing the uniform distribution of the gas phase in the gas-liquid mass transfer process, and proposes a device for uniformly distributing the gas-liquid two-phase in an eccentric jet bubbling reactor, which enhances the uniformity of gas-liquid distribution, increases the gas-liquid mass transfer area, and increases the gas-liquid mass transfer coefficient, thereby greatly improving the uniform mass transfer, heat transfer, and transmission process of the eccentric jet reactor, and providing a favorable contact place for the gas-liquid two-phase reaction in the reactor.

[0041] (3) The present invention provides a method and device for enhancing the uniform distribution of the gas phase in the gas-liquid mass transfer process. The material distribution in the reactor is uniform, and the fluctuation deviation distribution is 0.1 percentage point, which increases the gas content in the reactor by 1-30 percentage points and the gas-liquid mass transfer coefficient by 40-230 percentage points. BRIEF DESCRIPTION OF THE DRAWINGS

[0042] Figure 1The schematic diagram of the structure of a gas phase uniform distribution device for enhancing the gas-liquid mass transfer process in the present invention is shown, wherein ρ is the kinetic energy in the distribution pipeline and the density of the medium flowing through, and the unit is kg / m 3 ; v is the velocity of the fluid in the distribution pipe, in m / s; i, i-1, i+1 are the i-th, i-1, i+1-th positions, respectively, in dimensionless units; n, n-1 are the n-th and n-1-th outflow orifice numbers, in units; d is the diameter of the outflow orifice, in mm; S is the hole spacing, in mm; q1, q2, q3, q i-1 ,q i ,q i+1 ,q n-1 ,q n分别 is the flow rate of the 1st, 2nd, 3rd, i-1, i, i+1, n-1, and nth outflow orifices, in m 3 / s;u i is the flow velocity of the ith outflow orifice, in m / s; x is the position, in m; L is the length of the distribution pipe, in mm.

[0043] Figure 2 It shows a schematic diagram of flow rate changes in the gas phase uniform distribution device for enhancing the gas-liquid mass transfer process under different working conditions in the present invention, wherein a is a schematic diagram of flow rate distribution when the flow rate is ideal; b is a schematic diagram of flow rate distribution when momentum and kinetic energy are dominant; c is a schematic diagram of flow rate distribution when friction resistance is dominant; d is a schematic diagram of flow rate distribution when there is an upstream disturbance and kinetic energy is dominant.

[0044] FIG3 shows the material distribution in a gas phase uniform distribution device for enhancing gas-liquid mass transfer in the present invention. Figure 3a , 3b ,in, Figure 3a This is a material distribution diagram in the gas phase uniform distribution device used in Example 1; Figure 3b This is a material distribution diagram in the gas phase uniform distribution device used in Example 2; Figure 3c This is a material distribution diagram in the gas phase uniform distribution device used in Example 3; Figure 3d This is the material distribution diagram in the gas phase uniform distribution device used in Example 4. DETAILED DESCRIPTION

[0045] A first aspect of the present invention provides a method for uniformly distributing the gas phase in a gas-liquid mass transfer process, comprising the following steps:

[0046] 1) Take the distribution pipe and set the number of outflow orifices on the pipe wall according to formula (1).

[0047] The formula (1) is:

[0048] In the formula,

[0049] η is the porosity of the distribution pipe, unit is dimensionless;

[0050] n is the number of outflow orifices, pieces;

[0051] d is the diameter of the outflow orifice, mm;

[0052] D is the inner diameter of the distribution pipe, mm;

[0053] L is the length of the distribution pipe, mm;

[0054] 2) With respect to step 1), a distribution pipeline having an outflow orifice is obtained, and the Euler number Eu is calculated according to formula (2) to determine the gas phase uniformity of the distribution pipeline in step 1).

[0055] The formula (2) is:

[0056] In the formula,

[0057] Eu is the Euler number, and its unit is dimensionless;

[0058] X is the dimensionless number of length, and its unit is dimensionless;

[0059] v0 is the flow velocity at the outlet of the distribution pipe, in m / s;

[0060] g is the gravitational acceleration of the fluid, in m / s 2 ;

[0061] L is the length of the distribution pipe, mm;

[0062] E is the aspect ratio, dimensionless;

[0063] Re0 is the outlet Reynolds number of the distribution pipe, unit is dimensionless;

[0064] z is the characteristic parameter of the velocity distribution inside the distribution pipe of the porous fluid, and the unit is dimensionless;

[0065] α is the correction coefficient, specifically the momentum change rate of the fluid flowing through the first hole, or the momentum exchange coefficient of the first hole, which is 0.65;

[0066] β is the correction coefficient, which is the ratio of the porosity η and the aspect ratio E of the porous tube, β≈0.15;

[0067] 3) According to the Euler number Eu obtained in step 2), the pressure difference of the distribution pipeline is determined according to formula (3) to enhance the gas-liquid mass transfer process.

[0068] The formula (3) is:

[0069] In the formula,

[0070] Eu is the Euler number, and its unit is dimensionless;

[0071] P x is the pressure at x, in kPa;

[0072] P0 is the starting point pressure, in kPa;

[0073] ρ is the kinetic energy in the distribution pipe and the density of the medium flowing through it, in kg / m 3 ;

[0074] v0 is the flow velocity of the distribution pipe through the outlet orifice, in m / s.

[0075] In the above-mentioned gas phase uniform distribution method, in step 1), the opening ratio η of the distribution pipe is 0.0003-0.01.

[0076] In the above-mentioned gas phase uniform distribution method, in step 1), the inner diameter D of the distribution pipe is 5-800 mm, preferably 5-300 mm.

[0077] In the above-mentioned gas phase uniform distribution method, in step 2), in the formula (2), the X is calculated according to the formula (4),

[0078] The formula (4) is:

[0079] In the formula,

[0080] X is the dimensionless number of length, and its unit is dimensionless;

[0081] x is the distance between one end of the distribution pipe and the outflow orifice, in m;

[0082] L is the length of the distribution pipe, mm.

[0083] In a specific embodiment, when the distribution pipeline is a closed loop pipeline, in the formula (4), x = L, that is,

[0084] In the above-mentioned gas phase uniform distribution method, in step 2), in the formula (2), the E is calculated according to the formula (5),

[0085] The formula (5) is:

[0086] In the formula,

[0087] E is the aspect ratio, dimensionless;

[0088] L is the length of the distribution pipe, mm;

[0089] D is the inner diameter of the distribution pipe, mm.

[0090] In a specific embodiment, E is 5-500 mm, preferably 50-300 mm.

[0091] In the above-mentioned gas phase uniform distribution method, in step 2) or 3), the relative numerical value of the Euler number Eu can help judge the quality of the gas phase uniform distribution device.

[0092] In the above-mentioned gas phase uniform distribution method, in step 2), when the distribution pipeline is a closed-loop pipeline, X=1 in the formula (2), and the formula (6) is obtained,

[0093] The formula (6) is:

[0094] The meanings of the parameters in formula (6) are the same as those in formula (2).

[0095] In a specific embodiment, in the formula (2) or (6), g is calculated according to the formula (7),

[0096] The formula (7) is:

[0097] In the formula,

[0098] g is the gravitational acceleration of the fluid, in m / s 2 ;

[0099] ρ is the kinetic energy in the distribution pipe and the density of the medium flowing through it, in kg / m 3 ;

[0100] dp is the pressure gradient, in kPa;

[0101] dx is the interval of the infinitesimal element (x, x+dx), in m;

[0102] λ is the resistance coefficient along the way, unit is dimensionless;

[0103] D is the inner diameter of the distribution pipe, mm;

[0104] v is the velocity of the fluid in the distribution pipe, in m / s;

[0105] C f is the momentum exchange coefficient, unit is dimensionless;

[0106] dv is the differential of velocity, in m / s.

[0107] According to Bernoulli's theory, in general, when the outlet resistance is equal, the outlet flow rate is equal. When the flow rate is small, the inertial force can be ignored. When the flow rate increases, the inertial effect increases, the error increases, and the influence of momentum needs to be considered.

[0108] In a preferred embodiment, in the formula (7), the inner diameter D of the distribution pipe is 5-800 mm, preferably 5-300 mm.

[0109] In a preferred embodiment, in the formula (7), the C f According to formula (8),

[0110] The formula (8) is: f =2-k,

[0111] In the formula,

[0112] C f is the momentum exchange coefficient 1, unit is dimensionless;

[0113] k is the momentum exchange coefficient 2, and its unit is dimensionless.

[0114] In a further preferred embodiment, k is calculated according to formula (9):

[0115] The formula (9) is:

[0116] In the formula,

[0117] k is the momentum exchange coefficient 2, dimensionless;

[0118] α is the correction coefficient, specifically the momentum change rate of the fluid flowing through the first hole, or the momentum exchange coefficient of the first hole, which is 0.65;

[0119] β is the correction coefficient, which is the ratio of the porosity η and the aspect ratio E of the porous tube, β≈0.15;

[0120] v is the velocity of the fluid in the distribution pipe, in m / s;

[0121] v0 is the flow velocity of the distribution pipe through the outlet orifice, in m / s.

[0122] The k is the momentum exchange coefficient 2, which is a correction for the momentum component of the fluid leaving the orifice along the flow direction. The ratio of the momentum component of the fluid carried away by the orifice outflow along the flow direction to the mainstream momentum should be equal to the relative change rate of the mainstream momentum △v 2 / v 2 related.

[0123] In a further preferred embodiment, when z=1, formula (9) obtains formula (10):

[0124] The formula (10) is:

[0125] The meanings of the parameters in formula (10) are the same as those in formula (9).

[0126] In a preferred embodiment, in formula (7), λ is calculated according to formula (11):

[0127] The formula (11) is:

[0128] In the formula,

[0129] λ is the resistance coefficient along the way, unit is dimensionless;

[0130] Re is the general Reynolds number of the distribution pipe and its units are dimensionless.

[0131] In a further preferred embodiment, the Re satisfies 2000≤Re<10 5 .

[0132] In a further preferred embodiment, the Re is 2000-40000, preferably 2300-39000, more preferably 2500-38000.

[0133] The above-mentioned drag coefficient λ and general Reynolds number Re can be found in references, for example, Sun Zaizheng. A simplified method for calculating the drag coefficient along the way [J]. Journal of Shandong Textile Engineering Institute, 1988, (02): 19-23.

[0134] In a specific embodiment, in the formula (2) or (6), the outlet flow velocity v0 of the distribution pipe is 5.3-21.1 m·s -1 .

[0135] In a specific embodiment, in the formula (2) or (6), z is calculated according to the formula (12),

[0136] The formula (12) is:

[0137] In the formula,

[0138] z is the characteristic parameter of the velocity distribution inside the distribution pipe of the porous fluid, and the unit is dimensionless;

[0139] E is the aspect ratio, dimensionless;

[0140] η is the porosity of the distribution pipe, unit is dimensionless;

[0141] η i The inner diameter of the distribution pipe is D i , the diameter of the outflow orifice is d i and hole spacing S i The porosity at , in dimensionless units.

[0142] In a preferred embodiment, in the formula (12), the η i According to formula (13),

[0143] The formula (13) is:

[0144] In the formula,

[0145] D i is the inner diameter of the distribution pipe at the i-th outflow orifice position, mm;

[0146] d i is the diameter of the ith outflow orifice, mm;

[0147] S i is the hole spacing between the ith outflow orifice and the adjacent outflow orifice, mm.

[0148] In a preferred embodiment, in formula (12), when z>1, the flow in the porous fluid distribution pipe is controlled by friction resistance, and the flow velocity changes along the flow path presenting a trend of first fast and then slow; when z<1, the flow in the porous fluid distribution pipe is controlled by the fluid's own momentum, and the flow velocity changes along the flow path presenting a trend of first slow and then fast; when z=1, when the effects of momentum, gravity and friction resistance are balanced, the fluid pressure is evenly distributed along the flow path, the outflow from each orifice along the flow path is equal, and the flow velocity changes along the flow path is linear.

[0149] In a specific implementation, in the formula (2) or (6), the Re0 is calculated according to the formula (14),

[0150] The formula (14) is:

[0151] In the formula,

[0152] Re0 is the outlet Reynolds number of the distribution pipe, unit is dimensionless;

[0153] ρ is the kinetic energy in the distribution pipe and the density of the medium flowing through it, in kg / m 3 ;

[0154] v0 is the flow velocity of the distribution pipe through the outflow orifice, in m / s;

[0155] D is the inner diameter of the distribution pipe, mm;

[0156] μ is the dynamic viscosity coefficient, and its unit is Pa·s.

[0157] The v0 can be calculated based on the average outflow velocity of the outflow orifice in the distribution pipe, which can be approximated as the outflow velocity of the outflow orifice.

[0158] In a preferred embodiment, the outlet Reynolds number Re0 of the distribution pipe is 1950-11000, preferably 2050-10100.

[0159] In the above-mentioned gas phase uniform distribution method, in step 2) or 3), the Euler number Eu meets the formula (15),

[0160] The formula (15) is:

[0161] The meanings of the parameters in formula (15) are the same as those in formula (2).

[0162] The above formulas are used to illustrate the principle and method of gas phase uniform distribution in the process of enhancing gas-liquid mass transfer, among which formula (2) can better characterize the gas phase uniform distribution in the process of gas-liquid mass transfer and reveal the important physical parameters and operating parameters that affect the gas-liquid uniform distribution.

[0163] In the above-mentioned gas phase uniform distribution method, the outflow orifice flow rate of the distribution pipeline meets the formula (16),

[0164] The formula (16) is:

[0165] In the formula,

[0166] q is the outflow orifice flow rate of the distribution pipe;

[0167] d is the diameter of the outflow orifice, mm;

[0168] D is the inner diameter of the distribution pipe, mm;

[0169] η is the porosity of the distribution pipe, unit is dimensionless;

[0170] dv is the differential of velocity, in m / s;

[0171] dx is the interval of the infinitesimal element (x, x+dx), and its unit is m.

[0172] In a specific implementation, formula (16) is obtained by integrating formula (17),

[0173] The formula (17) is:

[0174] In the formula,

[0175] ρ is the kinetic energy in the distribution pipe and the density of the medium flowing through it, in kg / m 3 ;

[0176] D is the inner diameter of the distribution pipe, mm;

[0177] v is the velocity of the fluid in the distribution pipe, in m / s;

[0178] dv is the differential of velocity, in m / s;

[0179] dx is the interval of the infinitesimal element (x, x+dx), in m;

[0180] u is the flow velocity out of the outlet orifice, in m / s;

[0181] S is the hole spacing, in mm.

[0182] In the above formulas (16) and (17), the average outflow velocity of the small hole in the micro-element segment can be approximated to the outflow velocity of the small hole at the micro-element segment, and the continuity equation of the variable mass flow of the incompressible fluid is established. The specific flow rate change is shown in Figure 2 .

[0183] In the above-mentioned gas phase uniform distribution method, it is very important to ensure the uniform distribution of gas-liquid two-phase or even multi-phase in the reactor. As is known to all, the kinetic energy in a gas phase uniform distribution device such as a porous gas distribution tube or a gas distributor is not only related to the density ρ of the medium flowing through, the cross-sectional area A of the pipeline, and the flow velocity U in the tube; it is also related to the small hole pressure drop and the small hole resistance coefficient ζ0, the flow velocity v0 of the small hole, and the gravity acceleration g where the fluid is located. The above are the factors that affect the good performance of a gas phase uniform distribution device such as a porous gas distribution tube or a gas distributor. The key points are two points. One is the ratio of the kinetic energy in a gas phase uniform distribution device such as a porous gas distribution tube or a gas distributor to the small hole pressure drop, and the other is the ratio of the resistance loss in a gas phase uniform distribution device such as a porous gas distribution tube or a gas distributor to the small hole pressure drop. The resistance loss of a gas phase uniform distribution device such as a porous gas distribution tube or a gas distributor and the friction resistance coefficient in the distribution pipe, ζ k , the flow rate in the pipe and the gravity acceleration where the fluid is located. Generally, increasing the perforation pressure drop or reducing the opening ratio is conducive to the uniform distribution of the fluid, but if the opening ratio is too low, the opening area is too small, the hole spacing is too large, and dead angles are formed, it is not conducive to the uniform distribution of the fluid.

[0184] The second aspect of the present invention provides a gas phase uniform distribution device for enhancing the gas-liquid mass transfer process, including a distribution pipe with at least one outflow orifice. The distribution pipe with the outflow orifice complies with the above-mentioned gas phase uniform distribution method.

[0185] In the above-mentioned gas phase uniform distribution device, the shape of the distribution pipe can be a regular tube or an irregular tube, preferably a round tube or a square tube.

[0186] In the above-mentioned gas phase uniform distribution device, if Figure 1 As shown, the length of the distribution pipe is L, the diameter is D, the number of outflow orifices is n, the diameter of the outflow orifice is d, the hole spacing of the outflow orifice is S, the fluid velocity in the distribution pipe is v, the flow velocity out of the outflow orifice is u, η iThe pipe diameter is D i , opening diameter d i and hole spacing S i The opening rate at .

[0187] In the above-mentioned gas phase uniform distribution device, the opening ratio η of the distribution pipeline is 0.0003-0.01.

[0188] In the above-mentioned gas phase uniform distribution device, the inner diameter D of the distribution pipe is 5-800 mm, preferably 5-300 mm.

[0189] In the above-mentioned gas phase uniform distribution device, the aspect ratio E (ratio of length to inner diameter L / D) of the distribution pipe is 5-500 mm, preferably 50-300 mm.

[0190] In the above-mentioned gas phase uniform distribution device, the general Reynolds number Re of the distribution pipeline meets 200≤Re<10 5 .

[0191] In a specific embodiment, the Re is 2000-40000, preferably 2300-39000, and more preferably 2500-38000.

[0192] In the above-mentioned gas phase uniform distribution device, the outflow orifice flow velocity v0 of the distribution pipeline is 5.3-21.1 m·s -1 .

[0193] In the above-mentioned gas phase uniform distribution device, the outlet Reynolds number Re0 of the distribution pipe is 1950-11000, preferably 2050-10100.

[0194] In the above-mentioned gas phase uniform distribution device, the outlet orifice of the distribution pipeline is provided with a plurality of outlet orifice groups along the axial direction of the distribution pipeline, and the spacing distances between adjacent outlet orifice groups are equal, and the outlet orifice group is provided with a plurality of outlet orifices along the circumference of the distribution pipeline, and the spacing distances between adjacent outlet orifices are equal. That is, the outlet orifice divides the distribution pipeline into long tubes with equal cross-sections.

[0195] In the above-mentioned gas phase uniform distribution device, when the distribution pipeline is a closed-loop pipeline, x=L, that is,

[0196] The third aspect of the present invention provides the above-mentioned gas phase uniform distribution method for enhancing the gas-liquid mass transfer process, or the use of the above-mentioned gas phase uniform distribution device for enhancing the gas-liquid mass transfer process in enhancing the gas-liquid mass transfer process in a bubbling reactor.

[0197] A fourth aspect of the present invention provides a bubbling reactor comprising the gas phase uniform distribution device for enhancing the gas-liquid mass transfer process.

[0198] In the above bubbling reactor, the bubbling reactor is an eccentric jet bubbling reactor.

[0199] In the above bubbling reactor, the gas phase is input into the bubbling reactor through the gas phase uniform distribution device.

[0200] The following describes the embodiments of the present invention through specific examples, and those skilled in the art can easily understand other advantages and effects of the present invention from the contents disclosed in this specification. The present invention can also be implemented or applied through other different specific embodiments, and the details in this specification can also be modified or changed in various ways based on different viewpoints and applications without departing from the spirit of the present invention.

[0201] In the following examples, the rest of the raw materials or processing techniques, unless otherwise specified, are conventional commercially available raw materials or conventional processing techniques in the art.

[0202] Example 1

[0203] A gas phase uniform distribution device 1# is set in an eccentric jet bubbling reactor, and the specific structure is as follows: Figure 1 A distribution pipe is included, and the number of outflow orifices is set on the pipe wall of the distribution pipe according to formula (1), wherein the length of the distribution pipe is 10080 mm, the inner diameter D of the distribution pipe is 80 mm, the opening ratio η of the distribution pipe is 0.001, and the corresponding number of outflow orifices ranges from [200, 500]. The outflow orifice diameter can be obtained by inverse deduction from formula (1).

[0204] For the distribution pipeline with outflow orifice, the Euler number Eu is calculated according to formula (2) to determine the gas phase uniformity of the distribution pipeline. Since the distribution pipeline is a closed-loop pipeline, X = 1 in formula (2), that is, Eu is calculated according to formula (6) to be 0.62. Where, is 1000kg / m 3 , the Reynolds number Re of the distribution pipe is 11000, D is 80 mm, z is calculated as 1 according to formula (12). L is 10080 mm, and the flow velocity v0 of the distribution pipe through the outlet orifice is 8 m·s -1 , α is 0.65, β is 0.15, the ratio of the length to the inner diameter of the distribution pipe E=L / D is 126, and the Reynolds number of the outlet of the distribution pipe Re0=3700.

[0205] According to the obtained Euler number Eu, the pressure difference P of the distribution pipeline is determined according to formula (3): x -P0 is 40.24kPa, and the variance is ±20kPa.

[0206] The distribution of materials in the reactor is as follows Figure 3aAs shown, the material distribution is uniform, proving that the gas phase uniform distribution device 1# can achieve uniform gas-liquid distribution in the axial eccentric jet bubbling reactor. The changes in the gas holdup in the reactor, the gas holdup at the outlet, and the gas-liquid mass transfer coefficient are shown in Table 1.

[0207] Example 2

[0208] A gas phase uniform distribution device 2# is set in an eccentric jet bubbling reactor, and the specific structure is as follows Figure 1 A distribution pipe is included, and the number of outflow orifices is set on the pipe wall of the distribution pipe according to formula (1), wherein the length of the distribution pipe is 22600 mm, the inner diameter D of the distribution pipe is 200 mm, and the opening ratio η of the distribution pipe is 0.0017. The corresponding number of outflow orifices ranges from [100, 800]. The outflow orifice diameter can be obtained by inverse calculation of formula (1).

[0209] For the distribution pipeline with outflow orifice, the Euler number Eu is calculated according to formula (2) to determine the gas phase uniformity of the distribution pipeline. Since the distribution pipeline is a closed-loop pipeline, X = 1 in formula (2), that is, Eu is calculated according to formula (6) to be 0.62. Where ρ is 1200 kg / m 3 , the Reynolds number Re of the distribution pipe is 37000, D is 200 mm, k is calculated by formula (9), z is 1 calculated by formula (12), L is 22600 mm, and the flow velocity v0 of the distribution pipe through the outlet orifice is 11 m·s -1 , α is 0.65, β is 0.15, the ratio of the length to the inner diameter of the distribution pipe E=L / D is 113, and the Reynolds number of the outlet of the distribution pipe Re0=3500.

[0210] According to the obtained Euler number Eu, the pressure difference P of the distribution pipeline is determined according to formula (3): x -P0 is 91.30 kPa, and the variance is ±18 kPa. Compared with Example 1, although the pressure drop caused by the velocity increases, the variance of the pressure difference becomes smaller and the stability is improved after the distribution pipe structure is improved. The above design parameters and operating parameters can be used to enhance the gas-liquid mass transfer process.

[0211] The distribution of materials in the reactor is as follows Figure 3b As shown, the material distribution is uniform, proving that the gas phase uniform distribution device 2# can achieve uniform gas-liquid distribution in the axial eccentric jet bubbling reactor. The changes in the gas holdup in the reactor, the gas holdup at the outlet, and the gas-liquid mass transfer coefficient are shown in Table 1.

[0212] Example 3

[0213] A gas phase uniform distribution device 3# is set in an eccentric jet bubbling reactor, and the specific structure is as follows: Figure 1A distribution pipe is included, and the number of outflow orifices is set on the pipe wall of the distribution pipe according to formula (1), wherein the length of the distribution pipe is 12000 mm, the inner diameter D of the distribution pipe is 10 mm, the opening ratio η of the distribution pipe is 0.0027, and the corresponding number of outflow orifices ranges from [500, 800]. The outflow orifice diameter can be obtained by inverse calculation of formula (1).

[0214] For the distribution pipeline with outflow orifice, the Euler number Eu is calculated according to formula (2) to determine the gas phase uniformity of the distribution pipeline. Since the distribution pipeline is a closed-loop pipeline, X = 1 in formula (2), that is, Eu is calculated according to formula (6) to be 0.65. Where ρ is 1100 kg / m 3 , the Reynolds number Re of the distribution pipe is 28000, and D is 150 mm. z is calculated as 1 according to formula (12). L is 12000 mm, and the flow velocity v0 of the distribution pipe through the outlet orifice is 21 m·s -1 , α is 0.65, β is 0.15, the ratio of the length to the inner diameter of the distribution pipe E=L / D is 80, and the Reynolds number of the outlet of the distribution pipe Re0=3300.

[0215] According to the obtained Euler number Eu, the pressure difference P of the distribution pipeline is determined according to formula (3): x -P0 is 315.32 kPa, and the variance is ±15 kPa. Compared with Example 2, although the pressure drop caused by the velocity increases, the variance of the pressure difference becomes smaller after the distribution pipe structure is improved, and the stability is improved compared with Example 1. The above design parameters and operating parameters can be used to enhance the gas-liquid mass transfer process.

[0216] The distribution of materials in the reactor is as follows Figure 3c As shown, the material distribution in the reactor is uniform, proving that the gas phase uniform distribution device 3# can achieve uniform gas-liquid distribution in the axial eccentric jet bubbling reactor. The changes in gas holdup in the reactor, the changes in gas holdup at the outlet, and the changes in gas-liquid mass transfer coefficient are shown in Table 1.

[0217] Example 4

[0218] A gas phase uniform distribution device 4# is set in an eccentric jet bubbling reactor, and the specific structure is as follows: Figure 1 A distribution pipe is included, and the number of outflow orifices is set on the pipe wall of the distribution pipe according to formula (1), wherein the length of the distribution pipe is 6000 mm, the inner diameter D of the distribution pipe is 15 mm, the opening ratio η of the distribution pipe is 0.009, and the corresponding number of outflow orifices ranges from [20, 200]. The outflow orifice diameter can be obtained by inverse calculation of formula (1).

[0219] For the distribution pipeline with outflow orifice, the Euler number Eu is calculated according to formula (2) to determine the gas phase uniformity of the distribution pipeline. Since the distribution pipeline is a closed-loop pipeline, X = 1 in formula (2), that is, Eu is calculated according to formula (6) to be 0.58. Where ρ is 900 kg / m 3 , the Reynolds number Re of the distribution pipe is 2800, and D is 15 mm. z is calculated as 1 according to formula (12). L is 6000 mm, and the flow velocity v0 of the distribution pipe through the outlet orifice is 6 m·s -1 , α is 0.65, β is 0.15, the ratio of the length to the inner diameter of the distribution pipe E=L / D is 400, and the Reynolds number of the outlet of the distribution pipe Re0=8000.

[0220] According to the obtained Euler number Eu, the pressure difference P of the distribution pipeline is determined according to formula (3): x -P0 is 18.792 kPa, and the variance is ±5 kPa. Compared with Example 3, after the structure is optimized and the operating parameters are optimized, the variance of the pressure difference becomes smaller, and the stability is greatly improved compared with Examples 2 and 1. The above design parameters and operating parameters can be used to enhance the gas-liquid mass transfer process.

[0221] The distribution of materials in the reactor is as follows Figure 3d As shown, the material distribution in the reactor is uniform, proving that the gas phase uniform distribution device 4# can achieve uniform gas-liquid distribution in the axial eccentric jet bubbling reactor. The changes in gas holdup in the reactor, the changes in gas holdup at the outlet, and the changes in gas-liquid mass transfer coefficient are shown in Table 1.

[0222] Test Example 1

[0223] The changes in the gas holdup in the reactor, the gas holdup at the outlet, and the gas-liquid mass transfer coefficient in Examples 1-4 are shown in Table 1.

[0224] Table 1 Changes in gas holdup in the reactor, changes in gas holdup at the outlet and gas-liquid mass transfer coefficient

[0225]

[0226] As can be seen from Table 1, the gas distributor in the eccentric jet bubbling reactor prepared by a new gas phase uniform distribution method for enhancing the gas-liquid mass transfer process can significantly increase the gas holdup in the reactor and the gas holdup at the outlet, and greatly improve the gas-liquid mass transfer coefficient.

[0227] The above is only a preferred embodiment of the present invention, and is not any formal or substantial limitation of the present invention. It should be pointed out that ordinary technicians in this technical field can make several improvements and supplements without departing from the method of the present invention, and these improvements and supplements should also be regarded as the protection scope of the present invention. Any technician familiar with this profession, without departing from the spirit and scope of the present invention, can make some changes, modifications and evolutions of the technical content disclosed above, which are equivalent embodiments of the present invention; at the same time, any changes, modifications and evolutions of any equivalent changes made to the above embodiments based on the essential technology of the present invention are still within the scope of the technical solution of the present invention.

Claims

1. A method for uniformly distributing the gas phase in a gas-liquid mass transfer process, comprising the following steps: 1) Take the distribution pipe and set the number of outflow orifices on the pipe wall according to formula (1). The formula (1) is: In the formula, η is the porosity of the distribution pipe, unit is dimensionless; n is the number of outflow orifices, pieces; d is the diameter of the outflow orifice, mm; D is the inner diameter of the distribution pipe, mm; L is the length of the distribution pipe, mm; 2) With respect to step 1), a distribution pipeline having an outflow orifice is obtained, and the Euler number Eu is calculated according to formula (2) to determine the gas phase uniformity of the distribution pipeline in step 1). The formula (2) is: In the formula, Eu is the Euler number, and its unit is dimensionless; X is the dimensionless number of length, and its unit is dimensionless; v0 is the flow velocity at the outlet of the distribution pipe, in m / s; g is the gravitational acceleration of the fluid, in m / s 2 ; L is the length of the distribution pipe, mm; E is the aspect ratio, dimensionless; Re0 is the outlet Reynolds number of the distribution pipe, unit is dimensionless; z is the characteristic parameter of the velocity distribution inside the distribution pipe of the porous fluid, and the unit is dimensionless; α is the correction coefficient, specifically the momentum change rate of the fluid flowing through the first hole, or the momentum exchange coefficient of the first hole, which is 0.65; β is the correction coefficient, which is the ratio of the porosity η and the aspect ratio E of the porous tube, β≈0.15; 3) According to the Euler number Eu obtained in step 2), the pressure difference of the distribution pipeline is determined according to formula (3) to enhance the gas-liquid mass transfer process. The formula (3) is: In the formula, Eu is the Euler number, and its unit is dimensionless; P x is the pressure at x, in kPa; P0 is the starting point pressure, in kPa; ρ is the kinetic energy in the distribution pipe and the density of the medium flowing through it, in kg / m 3 ; v0 is the flow velocity of the distribution pipe through the outlet orifice, in m / s.

2. The method for enhancing the gas-liquid mass transfer process according to claim 1, characterized in that: In step 2), the formula (2) includes any one or more of the following conditions: A1) X is calculated according to formula (4), The formula (4) is: In the formula, X is the dimensionless number of length, and its unit is dimensionless; x is the distance between one end of the distribution pipe and the outflow orifice, in m; L is the length of the distribution pipe, mm; A2) The E is calculated according to formula (5): The formula (5) is: In the formula, E is the aspect ratio, dimensionless; L is the length of the distribution pipe, mm; D is the inner diameter of the distribution pipe, mm; A3) When the distribution pipeline is a closed loop pipeline, X=1 in the formula (2), and the formula (6) is obtained, The formula (6) is: The meanings of the parameters in formula (6) are the same as those in formula (2).

3. The method for enhancing the uniform distribution of the gas phase in the gas-liquid mass transfer process according to claim 2, characterized in that: The formula (2) or (6) includes any one or more of the following conditions: A31) The g is calculated according to formula (7), The formula (7) is: In the formula, g is the gravitational acceleration of the fluid, in m / s 2 ; ρ is the kinetic energy in the distribution pipe and the density of the medium flowing through it, in kg / m 3 ; dp is the pressure gradient, in kPa; dx is the interval of the infinitesimal element (x, x+dx), in m; λ is the resistance coefficient along the way, unit is dimensionless; D is the inner diameter of the distribution pipe, mm; v is the velocity of the fluid in the distribution pipe, in m / s; C f is the momentum exchange coefficient, unit is dimensionless; dv is the differential of velocity, in m / s; A32) The z is calculated according to formula (12), The formula (12) is: In the formula, z is the characteristic parameter of the velocity distribution inside the distribution pipe of the porous fluid, and the unit is dimensionless; E is the aspect ratio, dimensionless; η is the porosity of the distribution pipe, unit is dimensionless; η i The inner diameter of the distribution pipe is D i , the diameter of the outflow orifice is d i and hole spacing S i The opening ratio at , in dimensionless units; A33) The Re0 described above is calculated according to formula (14), The formula (14) is: In the formula, Re0 is the outlet Reynolds number of the distribution pipe, unit is dimensionless; ρ is the kinetic energy in the distribution pipe and the density of the medium flowing through it, in kg / m 3 ; v0 is the flow velocity of the distribution pipe through the outflow orifice, in m / s; D is the inner diameter of the distribution pipe, mm; μ is the dynamic viscosity coefficient, and its unit is Pa·s.

4. The method for enhancing the uniform distribution of the gas phase in the gas-liquid mass transfer process according to claim 3, characterized in that: Also includes any one or more of the following conditions: A311) In the formula (7), C f According to formula (8), The formula (8) is: f =2-k, In the formula, C f is the momentum exchange coefficient 1, unit is dimensionless; k is the momentum exchange coefficient 2, dimensionless; A312) In formula (7), λ is calculated according to formula (11), The formula (11) is: In the formula, λ is the resistance coefficient along the way, unit is dimensionless; Re is the general Reynolds number of the distribution pipe, dimensionless; A321) In the formula (12), the η i According to formula (13), The formula (13) is: In the formula, D i is the inner diameter of the distribution pipe at the i-th outflow orifice position, mm; d i is the diameter of the ith outflow orifice, mm; S i is the hole spacing between the ith outflow orifice and the adjacent outflow orifice, mm.

5. The method for enhancing the uniform distribution of the gas phase in the gas-liquid mass transfer process according to claim 4, characterized in that: In item A311), k is calculated according to formula (9): The formula (9) is: In the formula, k is the momentum exchange coefficient 2, dimensionless; α is the correction coefficient, specifically the momentum change rate of the fluid flowing through the first hole, or the momentum exchange coefficient of the first hole, which is 0.65; β is the correction coefficient, which is the ratio of the porosity η and the aspect ratio E of the porous tube, β≈0.15; v is the velocity of the fluid in the distribution pipe, in m / s; v0 is the flow velocity of the distribution pipe through the outlet orifice, in m / s.

6. A gas phase uniform distribution device for enhancing the gas-liquid mass transfer process, characterized in that: The invention comprises a distribution pipeline, wherein at least one outflow orifice is provided on the distribution pipeline, and the distribution pipeline with the outflow orifice conforms to the gas phase uniform distribution method for strengthening the gas-liquid mass transfer process as described in any one of claims 1-5.

7. The gas phase uniform distribution device for enhancing the gas-liquid mass transfer process according to claim 6, characterized in that: Includes any one or more of the following conditions: B1) The distribution pipeline may be in a regular tubular shape or an irregular tubular shape; preferably, the distribution pipeline may be in a round tubular shape or a square tubular shape; B2) the opening ratio η of the distribution pipe is 0.0003-0.01; B3) The inner diameter D of the distribution pipeline is 5-800 mm; B4) the aspect ratio E of the distribution pipeline is 5-500 mm; B5) The general Reynolds number Re of the distribution pipeline meets 2000≤Re<105; preferably, the Re is 2000-40000; B6) The outlet flow velocity v0 of the distribution pipeline is 5.3-21.1 m·s -1 ; B7) The outlet Reynolds number Re0 of the distribution pipe is 1950-11000; preferably, the Re0 is 2050-10100; B8) When the distribution pipeline is a closed loop pipeline, x = L, that is, 8. Use of the method for enhancing the gas-liquid mass transfer process according to any one of claims 1 to 5, or the device for enhancing the gas-liquid mass transfer process according to any one of claims 6 to 7 in enhancing the gas-liquid mass transfer process in a bubbling reactor.

9. A bubbling reactor, characterized in that: The invention comprises a gas phase uniform distribution device for enhancing the gas-liquid mass transfer process according to any one of claims 6-7.

10. The bubbling reactor according to claim 9, characterized in that The bubbling reactor is an eccentric jet bubbling reactor.

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