CN107403033B - Vertical radial flow adsorber structure optimization method - Google Patents
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Abstract
The invention discloses a high-efficiency vertical radial flow adsorber structure optimization method. The method specifically comprises the following steps: the method comprises the following steps: establishing an initial model of a vertical radial flow adsorber, and obtaining an initial flow field through numerical simulation calculation; calculating factors influencing the efficiency of the vertical radial flow adsorber; judging whether the optimal design is achieved or not according to the calculation result, and if all the influence factors are optimal, obtaining the optimal design parameters of the structure of the adsorber; if the optimal value is not reached, entering an optimization stage until the optimal value is reached; the numerical simulation result is compared with the experiment measurement result, the reliability of the simulation experiment is verified, the optimized numerical simulation result is compared with the original model, the adsorption efficiency is improved by 52.05%, and the high efficiency of the optimization design is verified.
Description
Technical Field
The invention relates to the field of gas separation and purification, in particular to a structure optimization method for a vertical radial flow adsorber.
Background
Industrial gases are the basic raw material of modern industry, being likened to industrial "blood". According to statistics, the conservative estimate of the global industrial gas growth rate in 2016 + 2018 is 7%, and by 2018, the global industrial gas market scale exceeds 1220 billion dollars, so that the demand is huge. At present, industrial gas is mainly obtained by air separation through a low-temperature method, and the method has the characteristics of high purity and low cost and is more suitable for large-scale industrial gas production.
Since air is a multi-component gas and cannot be directly separated from the raw gas, a pre-purification treatment is usually required, and the equipment used in the process is called an adsorber and generally comprises a horizontal bed adsorber, a vertical axial flow adsorber and a vertical radial flow adsorber. The vertical radial flow adsorber has small floor area and low energy consumption, and is more suitable for the development of large-scale air separation equipment. Due to transportation limitation, the diameter of the adsorber cannot be too large, the adsorption capacity can be improved only by increasing the height of the adsorber, and the ratio of the height of the adsorption bed layer to the equivalent diameter of the outer annular flow channel can be increased by increasing the height, so that the radial pressure drop of the bed layer is more complicated along the height change, the radial flow distribution in the adsorber is more uneven, and the utilization rate of the adsorbent is reduced.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a vertical radial flow adsorber structure optimization method for air separation equipment in the technical field of deep cooling, and the optimized adsorber has better treatment effect.
A method for optimizing the structure of a vertical radial flow adsorber comprises the following steps: step 1, establishing an initial model of a vertical radial flow adsorber, and obtaining an initial flow field through numerical simulation calculation; step 2, calculating factors influencing the efficiency of the vertical radial flow adsorber; step 3, according to the pressure drop uniformity of the inner and outer flow passages
In the formula, N is the calculated data number; Δ piStatic pressure at point i, Pa;
and expressing the static pressure average value Pa, judging whether the optimal state is reached, if the optimal design parameter is reached, using the absorber, and if the optimal design parameter is not reached, entering an optimization stage until the optimal state is reached.
The improvement is that the initial model in step 1 comprises an inlet, an outlet, a tank body, an inner porous pipe, a middle porous pipe, an outer porous pipe, a bottom spherical cap seal head, a first non-porous steel ring, a second non-porous steel ring, a third non-porous steel ring, a bearing channel steel and a central flow channel distributor, wherein an outer flow channel is arranged between the outer porous pipe and the tank body, an inner flow channel is arranged between the inner porous pipes, the inlet is positioned at the lower end of the tank body, the outlet is positioned at the upper end of the tank body, the lower ends of the inner porous pipe, the middle porous pipe and the outer porous pipe are all welded on the bottom spherical cap seal head, the upper ends of the inner porous pipe, the middle porous pipe and the outer porous pipe are respectively connected with the first non-porous steel ring, the second non-porous steel ring and the third non-porous steel ring, an interlayer between the outer porous pipe and the middle porous pipe is a first adsorption area, an interlayer between the middle porous pipe and the, the bearing channel steel is positioned at the top of the tank body and corresponds to the outer flow channel, a cavity between the outer porous pipe and the inner wall of the tank body is the outer flow channel, porous media are filled in the cavity between the inner porous pipe and the outer porous pipe to serve as an adsorption layer, and the cavity surrounded by the inner porous pipe is a central flow channel.
The improvement is that the filler in the first adsorption zone is activated alumina adsorbent, and the filler in the second adsorption zone is molecular sieve adsorber.
The improvement is that when the initial flow field is calculated in the step 1, the adsorption isothermal equation adopts a Dubinin-Astakhov model, namely
Wherein
Wherein m represents the distribution of adsorption energy of the adsorbent; v is the volume of gas adsorbed per unit mass of adsorbent, m3；V0Is of finite micro volume, m3(ii) a R is a gas constant, J/(mol. K); t is absolute temperature, K; f is the adsorbent surface energy distribution function; beta is an empirical parameter.
As an improvement, the height-diameter ratio of the outer flow passage determines the model of the adsorber, when lambda L/(lambda L)/(lambda)6Dek)<<1, the absorber belongs to a momentum exchange control model; when λ L/(6D)ek)>>1, time; the adsorber belongs to a friction resistance control model, and when lambda L/(6D)ek)<At 1, the adsorber belongs to a momentum exchange dominant model; when λ L/(6D)ek)>When 1, the absorber belongs to a friction resistance dominant model, wherein lambda is a friction resistance coefficient; l is the length of the outer runner pipe, m; deIs the equivalent diameter, m; k is a momentum exchange coefficient, and since the two values of λ and k are generally closer, the flow model mainly depends on 6Dek value, adsorption efficiency of adsorber to maximize, D of adsorbereAnd L is larger, the outer flow passage belongs to a friction control type model, and the radial pressure drop of the inner flow passage and the outer flow passage of the adsorber generally shows a change rule of firstly decreasing and then increasing.
As a modification, the factors described in step 2 are porosity, inner runner sectional area, outer runner sectional area, and structure of the center runner distributor.
In a further improvement, the porosity is respectively determined by an inertia resistance coefficient of the outer hole pipe and an inertia resistance coefficient of the inner hole pipe, wherein the inertia resistance coefficient C2Is calculated by the formula
In the formula, C1The empirical value is taken as 0.62; dx is the plate thickness, m;
is the porosity.
In a further refinement, the configuration of the center flow distributor is controlled by the diameter and length, including the diameter of the top circle and the diameter of the bottom circle.
The further improvement is that the central flow channel distributor is a hollow cylinder, a hollow cone or a hollow circular truncated cone.
The central flow channel distributor is divided into two parts, wherein the upper part is a hollow cylinder, the lower part is a solid circular truncated cone, the upper part and the lower part are connected through a cylinder of a hollow perforated pipe or a wire mesh enclosure, and the diameter of the cylinder of the upper part, the diameter of the perforated pipe or the wire mesh enclosure is equal to the diameter of the top surface of the lower part.
As an improvement, the structural regulation of the center flow channel distributor comprises the following steps: the first step, overall optimization, considering the diameters of the upper distributor and the lower distributor to be equal, and optimizing three variables: the diameter, the length of an upper distributor and the length of a lower distributor are judged whether to reach the optimal design, if so, the optimal design parameters of the adsorber are obtained, otherwise, the local optimization stage is carried out; and secondly, carrying out local optimization aiming at the deficiency of the overall optimization, and further obtaining final optimization parameters.
The further improvement is that the local optimization means that the central flow channel distributor is divided into two parts of 0-0.5h and 0.5h-h equally, wherein h is the length of the central flow channel and the unit is m.
Has the advantages that:
the invention is a numerical simulation method, and has lower cost and higher efficiency in the process of structure optimization; the result of the numerical simulation is compared with the experimental measurement result, so that the reliability of the simulation experiment is verified; the process of heat and mass transfer during adsorption is calculated and considered, and the change of the flow field of the adsorber is calculated more accurately; three factors influencing the adsorption efficiency of the adsorber are considered simultaneously, the influence degree of each factor is disclosed more comprehensively, and design parameters of the adsorber are comprehensively researched; and finally, comparing the optimized model with the original model, and verifying the effectiveness of the optimized design.
Drawings
Fig. 1 is a schematic diagram of an initial model of an adsorber, wherein an inlet 1, an outlet 2, a tank body 3, an inner porous pipe 4, an outer porous pipe 5, a molecular sieve adsorption bed 6, an alumina adsorption bed 7, a bottom spherical cap seal head 8, a first non-porous steel ring 9, a second non-porous steel ring 10, a third non-porous steel ring 11 and a bearing channel steel 12.
FIG. 2 is a flow chart of the optimization of the method of the present invention;
FIG. 3 is a graph comparing simulated calculations with experimental measurements;
FIG. 4 is a graph of normalized alumina bed degradation uniformity for different porosities;
FIG. 5 is a graph of normalized bed pressure drop uniformity for different diameters;
FIG. 6 is a graph of the relationship between the structure of the center flow channel distributor and the uniformity of the pressure drop across the bed obtained by the global optimization method, wherein a is a graph showing the relationship between the uniformity of the pressure drop across the bed and the lengths of the upper distributor and the lower distributor when the diameter of the center flow channel distributor is 0.18 m; b, showing the relationship between the bed pressure drop uniformity and the lengths of the upper distributor and the lower distributor when the diameter of the distributor is 0.20 m; c, showing the relationship between the pressure drop uniformity of the bed layer and the lengths of the upper distributor and the lower distributor when the diameter of the distributor is 0.22 m;
FIG. 7 is a normalized graph of bed pressure drop uniformity for an optimal design configuration of a center flow channel distributor using global optimization;
FIG. 8 is a graph of the correlation of the center flow distributor structure with the uniformity of the bed pressure drop obtained by the local optimization method, wherein a is a graph of the length of the lower distributor obtained by the local optimization method with the uniformity of the bed pressure drop; b is a relation graph of the diameter of a lower distributor and the uniformity of bed pressure drop obtained by a local optimization method; and c is a relationship graph of the length of the upper distributor and the uniformity of the bed pressure drop obtained by a local optimization method.
FIG. 9 is a normalized pressure drop uniformity curve for the optimum design of the distributor using a local optimization method;
fig. 10 is a schematic diagram of an optimized model, wherein the distributor 13 is an upper hollow cylinder, the distributor 14 is a lower solid cone, and the hollow cylinder 15 is a porous cylinder.
FIG. 11 is a graph comparing an optimally designed model penetration curve with an initial model penetration curve, where a denotes CO2A total process diagram of gas breakthrough; b represents CO2Partial enlargement upon gas breakthrough.
Detailed Description
The technical scheme of the invention is described in detail in the following by combining the attached drawings and the embodiment.
Example 1 an initial model of a vertical radial flow adsorber is established, and an initial flow field is obtained by numerical simulation calculation
As shown in fig. 1, the initial model of the adsorber is a schematic structural diagram, the initial model includes an inlet, an outlet, a tank body, an inner porous pipe, a middle porous pipe, an outer porous pipe, a bottom spherical cap seal head, a first non-porous steel ring, a second non-porous steel ring, a third non-porous steel ring, a bearing channel steel, a central flow channel distributor, an outer flow channel is arranged between the outer porous pipe and the tank body, an inner flow channel is arranged between the inner porous pipes, the inlet is positioned at the lower end of the tank body, the outlet is positioned at the upper end of the tank body, the lower ends of the inner porous pipe, the middle porous pipe and the outer porous pipe are all welded on the bottom spherical cap seal head, the upper ends are respectively connected with the first non-porous steel ring, the second non-porous steel ring and the third non-porous steel ring, an interlayer between the outer porous pipe and the middle porous pipe is a first adsorption zone, an interlayer between the middle porous pipe and the inner porous pipe is, the bearing channel steel is positioned at the top of the tank body and corresponds to the outer flow channel, a cavity between the outer porous pipe and the inner wall of the tank body is the outer flow channel, porous media are filled in the cavity between the inner porous pipe and the outer porous pipe to serve as an adsorption layer, and the cavity surrounded by the inner porous pipe is a central flow channel. The inlet and outlet diameters are 0.20m, the tank body diameter is 0.84m, the inner porous pipe and the outer porous pipe have diameters of 0.2986m and 0.7586m respectively, the thicknesses of the molecular sieve and the alumina bed layer are 0.19m and 0.04m respectively, the lengths of the first non-porous steel ring, the second non-porous steel ring and the third non-porous steel ring are 0.2612m, 0.2236m and 0.2036m respectively, and other relevant parameters are shown in the figure.
Example 2 calculation of factors affecting the efficiency of a vertical radial flow adsorber
Fig. 2 is a flow chart of an optimization method of the present invention, and the optimization mainly comprises three steps: the method comprises the following steps of optimizing porosity, optimizing the cross section area of an outer runner, optimizing the cross section area of an inner runner and optimizing the structure of a central runner distributor, wherein the optimization of the porosity comprises the optimization process of the porosity of an outer hole pipe and the porosity of an inner hole pipe, the central runner distributor comprises a lower distributor and an upper distributor, the structure of the lower distributor to be optimized mainly comprises three variables of top surface circle diameter, bottom surface circle diameter and length, due to the constraint of assembly and manufacture, the top surface circle diameter and the bottom surface circle diameter of the upper distributor are equal to the top surface circle diameter of the lower distributor, the variable of the upper distributor to be optimized only has the length, when all the variables are in the optimal state, the system reaches the optimal state, and at the moment, all the variables are the optimal design parameters of the distributor.
Example 3 according to the uniformity of bed pressure drop, judging whether the optimum state is reached, if the optimum design parameter is reached, using the adsorber, if the optimum design parameter is not reached, entering the optimization stage until the optimum state is reached
The bed pressure drop uniformity refers to the difference between the static pressure of the inner runner and the static pressure of the outer runner.
For example, fig. 3 is a comparison graph of a simulation calculation result and an experimental measurement value, modeling is performed according to an adsorber used in an experiment, related parameters are set, calculation is performed by using the calculation method of the present invention, and finally, the calculation result is compared with the experimental measurement result.
When calculating, the flow is 2000m3/h，CO2The processing gas with the concentration of 400ppm and the temperature of 293K enters from the inlet, radially passes through the outer porous pipe, the first adsorption region, the middle porous pipe, the second adsorption region and the inner porous pipe, is collected in the central flow passage and then is discharged from the outlet, and in the process, the porosity, the sectional area of the inner flow passage, the sectional area of the outer flow passage and the structure of the central flow passage distributor have a great influence on the uniform distribution of the fluid.
As can be seen from fig. 3, the calculated penetration curve and the experimentally measured penetration curve both agree well with each other in the point of time of penetration and in the tendency of penetration, verifying the reliability of the method of the present invention.
FIG. 4 is a graph showing the pressure drop variation of the normalized alumina bed corresponding to different porosities of the inner perforated tube and the outer perforated tube, which shows that the porosity of the inner perforated tube and the outer perforated tube is reduced during the adsorption process, and the air flow uniformity of the molecular sieve bed and the alumina bed is greatly improved; the porosity of the outer porous pipe is reduced, the flow field uniformity of the molecular sieve bed layer is improved, but the flow field uniformity of the alumina bed layer is improved after being slightly reduced, specific numerical values are shown in table 1, and the porosity of the inner porous pipe and the porosity of the outer porous pipe which are optimal can be obtained through data and are respectively 0.30 and 0.435.
TABLE 1 uniformity of bed pressure drop as a function of porosity
Fig. 5 is a graph showing normalized pressure drop variation corresponding to the inner and outer flow channel cross-sectional areas, and it can be seen from the graph that the pressure drop of the bed layer shows a rule of decreasing first and then increasing in the adsorption process, the influence of the flow field uniformity by the outer flow channel cross-sectional area compared with the inner flow channel cross-sectional area is larger, the specific numerical values are shown in table 2, and the optimal inner and outer flow channel cross-sectional areas obtained from the data are 0.27m and 0.84m respectively.
TABLE 2 variation of bed pressure drop uniformity with inner and outer flow passage cross-sectional areas
FIG. 6 is a graph of the relationship between the structure of the center flow channel distributor and the uniformity of the pressure drop in the bed layer, which is obtained by the overall optimization method, wherein the diameters of the upper distributor and the lower distributor are assumed to be the same, and cylindrical distributors are adopted, and a, b and c represent the relationship between the length of the center distributor and the pressure drop when the diameters are respectively 0.18m, 0.20m and 0.22 m. The relationship between the distributor diameter and the lengths of the upper and lower portions was calculated as shown in Table 3, and it was confirmed that the uniformity of bed pressure drop was maximized when the diameter of the top circle was 0.20 m.
TABLE 3 influence of different upper and lower distributor lengths on the bed pressure drop uniformity for different distributor diameters
Fig. 7 is a bed pressure drop uniformity normalization curve obtained by an integral optimization method under the optimal design structure of the central flow channel distributor, and it can be known from the graph that after the integral optimization, the pressure drop uniformity is higher than that of the original model and is more approximate to an ideal curve of uniform distribution of air flow.
Fig. 8 is a graph of the relationship between the structure of the center flow channel distributor and the uniformity of the pressure drop in the bed layer, which is obtained by the local optimization method, in the local optimization, for the convenience of the assembly process, the upper distributor is considered to be a hollow cylinder, the diameter of the top circle of the lower distributor is equal to the diameter of the upper distributor, and is 0.20m, wherein a and b respectively represent the graphs of the influence of the diameter of the bottom circle of the lower distributor and the length of the distributor on the uniformity of the pressure drop in the bed layer, which are obtained by the local optimization method, and c represents the graph of the influence of the length of the upper distributor on the pressure drop. The influence of the lower distributor on the pressure drop uniformity at a height of 0.4m to 1.0m is obtained by calculation, as shown in table 4, and the influence of the upper distributor on the pressure drop uniformity at a height of 1.0m to 1.6m is obtained, as shown in table 5, and the optimal design parameters of the distributors can be obtained from the two tables.
TABLE 4 influence of lower distributor on uniformity of pressure drop across bed at height of 0.4m to 1.0m
TABLE 5 influence of upper distributor on uniformity of pressure drop across bed at height of 1.0m to 1.6m
Fig. 9 is a pressure drop uniformity normalization curve under the optimal design structure of the distributor obtained by using a local optimization method, and it can be known from the graph that after local optimization, the pressure drop uniformity is more uniform on the basis of overall optimization, mainly represented by the lower part and the upper part of the adsorber, and the pressure drop of the lower part and the upper part is closer to the ideal curve of gas flow uniform distribution than the pressure drop of the overall optimization.
FIG. 10 is a schematic diagram of an optimized design model in which the upper sparger is a hollow cylinder of 0.20m diameter and 0.54m length with an adsorber outlet connected at the upper end; the lower distributor is a solid round table body, the diameter of a top circle is 0.20m, the diameter of a bottom circle is 0.25m, the length is 0.37m, and the bottom surface is welded on the spherical cap end enclosure; the upper distributor and the lower distributor are connected by a porous hollow cylindrical pipe, the porous hollow cylindrical pipe can be replaced by a silk screen, the purpose is to prevent dust impurities from being discharged from an outlet and to ignore the influence of the dust impurities on the uniformity of a flow field of the adsorber, and the connection of other parts is the same as that of an initial model.
FIG. 11 is a graph comparing an optimally designed model penetration curve with an initial model penetration curve, a representing CO2The whole process diagram of gas breakthrough, b denotes CO2Partial enlargement upon gas breakthrough. CO 22The impurity gas with the highest content in the treated air firstly penetrates in the adsorption process, and the switching time of the adsorber is determined by CO2The breakthrough time was determined and it is evident from the a-plot that the breakthrough time of the adsorber after optimization is significantly delayed. Export of CO is generally considered in engineering2If the concentration exceeds 1ppm, the breakthrough is determined, the desorption process is carried out, as can be seen from the b diagram, the breakthrough time of the original model is 564s, and the breakthrough time of the optimized model is 1175s, and the CO of the original model is calculated2The adsorption capacity is 5.590mol, the adsorption capacity of the optimized model is improved to 11.657mol, the adsorption efficiency is improved by 52.05%, and the effectiveness of the optimization design is verified.
Claims (6)
1. A method for optimizing the structure of a vertical radial flow adsorber is characterized by comprising the following steps: step 1, establishing an initial model of a vertical radial flow adsorber, wherein the initial model comprises an inlet, an outlet, a tank body, an inner perforated pipe, a middle perforated pipe, an outer perforated pipe, a bottom spherical crown head, a first non-perforated steel ring, a second non-perforated steel ring, a third non-perforated steel ring, a bearing channel steel and a central flow channel distributor, an outer flow channel is arranged between the outer perforated pipe and the tank body, and an inner perforated pipe is arranged between the outer perforated pipe and the tank bodyThe inner flow channel is arranged between the inner porous pipe and the outer porous pipe, the inlet is positioned at the lower end of the tank body, the outlet is positioned at the upper end of the tank body, the lower ends of the inner porous pipe, the middle porous pipe and the outer porous pipe are all welded on the bottom spherical crown sealing head, the upper ends of the inner porous pipe, the middle porous pipe and the outer porous pipe are respectively connected with a first non-porous steel ring, a second non-porous steel, the interlayer of the outer porous pipe and the middle porous pipe is a first adsorption area, the interlayer of the middle porous pipe and the inner porous pipe is a second adsorption area, the first non-porous steel ring, the second non-porous steel ring and the third non-porous steel ring are hung at the inner top of the tank body, the bearing channel steel is positioned at the top of the tank body and corresponds to the outer flow channel, the cavity between the outer porous pipe and the inner wall of the tank body is an outer flow passage, the cavity between the inner porous pipe and the outer porous pipe is filled with porous media as an adsorption layer, a cavity of the inner porous pipe surrounding city is a central flow channel, and an initial flow field is obtained through numerical simulation calculation; step 2, calculating factors influencing the efficiency of the vertical radial flow adsorber, including porosity, inner runner sectional area, outer runner sectional area and structure of a central runner distributor, wherein the central runner distributor is composed of a hollow cylinder, a hollow truncated cone or a hollow cone, the structure of the central runner distributor is controlled by diameter and length, and the diameter includes the diameter of a top surface circle and the diameter of a bottom surface circle; step 3, calculating a formula according to the pressure drop uniformity of the inner and outer runners
In the formula, N is the calculated data number; Δ piStatic pressure at point i, Pa;
expressing the static pressure mean value Pa, judging whether an optimal state is reached, if the optimal design parameter is reached, using an absorber, and if the optimal design parameter is not reached, entering an optimization stage: the first step, overall optimization, considering the diameters of the upper distributor and the lower distributor to be equal, and optimizing three variables: the diameter, the length of an upper distributor and the length of a lower distributor are judged whether to reach the optimal design, if so, the optimal design parameters of the adsorber are obtained, otherwise, the local optimization stage is carried out; second, local optimization is performed to overcome the defects of the overall optimizationAnd transforming to obtain the final optimized parameters until the optimized state is reached.
2. The method of claim 1, wherein the packing in the first adsorption zone is activated alumina adsorbent and the packing in the second adsorption zone is molecular sieve adsorber.
3. The method of claim 1, wherein the initial flow field is calculated in step 1, and the adsorption isotherm equation is modeled by a Dubinin-Astakhov model
Wherein
Wherein m represents the distribution of adsorption energy of the adsorbent; v is the volume of gas adsorbed per unit mass of adsorbent, m3；V0Is of finite micro volume, m3(ii) a R is a gas constant, J/(mol. K); t is absolute temperature, K; f is the adsorbent surface energy distribution function; beta is an empirical parameter.
4. The method of claim 1, wherein the height-to-diameter ratio of the outer flow channels determines a model of the adsorber when λ L/(6D)ek)<<1, the absorber belongs to a momentum exchange control model; when λ L/(6D)ek)>>1, time; the adsorber belongs to a friction resistance control model, and when lambda L/(6D)ek)<At 1, the adsorber belongs to a momentum exchange dominant model; when λ L/(6D)ek)>When 1, the absorber belongs to a friction resistance dominant model, wherein lambda is a friction resistance coefficient; l is the length of the outer runner pipe, m; deIs the equivalent diameter, m; k is the momentum exchange coefficient.
5. The method of claim 1 wherein the vertical radial flow adsorber comprises a vertical flow adsorber, and a vertical flow adsorberCharacterized in that the porosity respectively determines the inertia resistance coefficient of the outer hole pipe and the inertia resistance coefficient of the inner hole pipe, wherein the inertia resistance coefficient C2Is calculated by the formula
In the formula, C1The empirical value is taken as 0.62; dx is the plate thickness, m;
is the porosity.
6. The method of claim 1, wherein the local optimization is performed by dividing the center channel distributor into two parts, i.e., 0-0.5h and 0.5h-h, h is the length of the center channel and is expressed in m.
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| US6701236B2 (en) * | 2001-10-19 | 2004-03-02 | Yamaha Hatsudoki Kabushiki Kaisha | Intelligent mechatronic control suspension system based on soft computing |
| CN104772004A (en) * | 2015-03-27 | 2015-07-15 | 浙江大学 | Large-flow vertical radial flow adsorption device with characteristic of layered parallel connection design, and method thereof |
| CN106844974A (en) * | 2017-01-24 | 2017-06-13 | 武汉旭日华环保科技股份有限公司 | The method and device of absorber optimization |
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| CN104772004A (en) * | 2015-03-27 | 2015-07-15 | 浙江大学 | Large-flow vertical radial flow adsorption device with characteristic of layered parallel connection design, and method thereof |
| CN106844974A (en) * | 2017-01-24 | 2017-06-13 | 武汉旭日华环保科技股份有限公司 | The method and device of absorber optimization |
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