Absorption method of acid-containing gas and application thereof

Abstract

The invention relates to the technical field of gas separation, and particularly discloses an acid-containing gas absorption method and application thereof. The absorption method comprises the following steps: in an absorption tower, enabling to-be-treated gas containing acid gas to be in contact with alkali liquor, and designing the diameter and the filler height of the absorption tower according to the number and the connection mode of the absorption tower and the gas inflow of the to-be-treated gas. The diameter of the absorption tower and the height of the filler designed by the technical method provided by the invention can realize efficient absorption of the acid gas in the actual production process. The absorption method provided by the invention is especially suitable for removing hydrogen sulfide in oil and gas fields.

Description

Technical Field

[0001] This invention relates to the field of gas separation technology, and more specifically to a method for absorbing acidic gases and its application. Background Technology

[0002] In some domestic oilfields, associated gas and gas production are accompanied by large amounts of toxic hydrogen sulfide gas, which not only causes severe corrosion of production equipment but also poses a significant threat to the personal safety of workers. With increasingly stringent requirements for safety and environmental protection, and strict regulations governing the hydrogen sulfide content of natural gas and locations involving hydrogen sulfide, natural gas desulfurization is an indispensable process in natural gas extraction and production.

[0003] Currently, common natural gas desulfurization methods in the petroleum industry mainly employ chemical absorption methods such as complex iron method, alkanolamine method, and iron oxide method. These methods suffer from problems such as complex processes, high operation and maintenance costs, and non-renewable desulfurizing agents. Biological desulfurization methods using alkaline solutions as hydrogen sulfide absorbents show promising application prospects in the petroleum industry. Summary of the Invention

[0004] The purpose of this invention is to provide a method for absorbing acidic gases. This method can effectively calculate the key design parameters of the acidic gas absorption device and has the characteristics of high efficiency, safety and stability, and low cost. It is particularly suitable for the removal of hydrogen sulfide in oil and gas fields.

[0005] According to a first aspect of the present invention, the present invention provides a method for absorbing acidic gas, the method comprising: contacting the gas to be treated containing acidic gas with an alkaline solution in an absorption tower; designing the absorption towers according to the number and connection method of the absorption towers and based on the inlet flow rate of the gas to be treated, wherein the design satisfies: Q is expressed in m 3 / d represents the unit value corresponding to the gas intake volume to be treated; D is the diameter of the absorption tower, in meters; H is the height of the absorption tower packing, in meters; k ranges from 1.1 to 1.3; the diameter D and the packing height H of the absorption tower satisfy: D = (M + N * Q) * k; M is 0.1-0.4; N is 0.00005-0.0001; H = (a + b * Q) * k; a is 2-6; b is 0.0002-0.0008.

[0006] According to a second aspect of the present invention, the present invention provides the application of the absorption method of the present invention in the removal of hydrogen sulfide in oil and gas fields.

[0007] Based on the above technical solutions and the associated gas situation of high hydrogen sulfide content in Jiangsu Oilfield, the technical methods provided by this invention are used to design the size and packing height of hydrogen sulfide absorption towers for some sites, and to achieve efficient absorption in actual production processes, so that the hydrogen sulfide concentration in the outlet gas is less than 20 ppm, and optimally less than 5 ppm. Attached Figure Description

[0008] Figure 1 This is an absorption system according to one embodiment of the present invention.

[0009] Explanation of reference numerals in the attached figures

[0010] 1-Gas storage tank; 2-Gas mixing tank with temperature control unit; 3-Air compressor; 4-Precision gas flow meter; 5-Precision pressure gauge; 6-Rich liquid tank; 7-Absorption tower; 8-Drying column; 9-Acid gas analyzer; 10-Thermometer; 11-Differential pressure gauge; 12-Alkali tank; 13-Metering pump Detailed Implementation

[0011] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0012] This invention provides a method for absorbing acidic gases. The method includes: contacting the acidic gas to be treated with an alkaline solution in an absorption tower; designing the absorption towers according to the number and connection method of the absorption towers and the inlet flow rate of the gas to be treated, wherein the design satisfies: Q is expressed in m... 3 / d represents the unit value corresponding to the gas intake volume to be treated; D is the diameter of the absorption tower, in meters; H is the height of the absorption tower packing, in meters; k ranges from 1.1 to 1.3; the diameter D and the packing height H of the absorption tower satisfy: D = (M + N * Q) * k; M is 0.1-0.4; N is 0.00005-0.0001; H = (a + b * Q) * k; a is 2-6; b is 0.0002-0.0008.

[0013] In this invention, the design of D and H is based on the total amount of gas to be treated Q, and can be optimized according to different series and parallel connection modes of the absorption towers.

[0014] According to a preferred embodiment of the present invention, when the absorption tower is in single-tower mode, and the diameter and packing height of the absorption tower satisfy: D=(0.36+0.0000893*Q)*k;H=(5.19+0.000608*Q)*k, the absorption tower has a better absorption effect on acidic gases, which can be controlled within 0-5ppm.

[0015] According to a preferred embodiment of the present invention, when the absorption tower is a two-tower series configuration, and the diameter and packing height of each absorption tower satisfy the following conditions: D = (0.31 + 0.0000754 × Q) * k; H = (3.9 + 0.000554 × Q) * k, the absorption tower exhibits better absorption efficiency for acidic gases, which can be controlled within 0-5 ppm. In this invention, the two-tower series configuration can be fed from one tower or from both towers. Preferably, both the gas to be treated containing acidic gases and the alkaline solution are fed from the first tower.

[0016] According to a preferred embodiment of the present invention, when the absorption tower is configured as a two-tower parallel system, and the diameter and packing height of each absorption tower satisfy the following conditions: D = (0.33 + 0.0000921 * Q) * k; H = (2.51 + 0.000617 * Q) * k, the absorption tower exhibits better absorption performance for acidic gases, which can be controlled within 0-5 ppm. In this invention, the throughput of each tower can be flexibly adjusted in the two-tower parallel system. For this invention, the throughput ratio of the first tower to the second tower is preferably 0.1-10:1, and more preferably, the throughputs of the first tower and the second tower are the same.

[0017] According to a preferred embodiment of the present invention, when the absorption tower is a three-tower series configuration, and the diameter and packing height of each absorption tower satisfy the following conditions: D = (0.23 + 0.0000573 * Q) * k; H = (2.84 + 0.000454 * Q) * k, the absorption tower achieves better absorption of acidic gases, which can be controlled within 0-5 ppm. In this invention, the three-tower series configuration can be fed from one tower or from all three towers. Preferably, the gas to be treated containing acidic gases and the alkaline solution are both fed from the first tower.

[0018] According to a preferred embodiment of the present invention, when the absorption tower is in a four-tower configuration, wherein two towers are connected in series and then in parallel, and the diameter and packing height of each absorption tower satisfy the following conditions: D = (0.17 + 0.0000372 * Q) * k; H = (2.046 + 0.000291 * Q) * k, the absorption tower exhibits better absorption efficiency for acidic gases, which can be controlled within 0-5 ppm. In this invention, when the absorption tower is in a four-tower configuration, wherein two towers are connected in series and then in parallel, the processing capacity of each parallel unit can be flexibly adjusted. For this invention, the preferred ratio of the processing capacities of each parallel unit is 0.1-10:1, and more preferably, the processing capacities of each parallel unit are the same. Each parallel unit can be fed from one of the towers or from two of the towers together, preferably from the first tower of each parallel unit.

[0019] In this invention, the processing capacity refers to the total amount of the acidic gas to be treated and the alkaline solution fed into the system.

[0020] In this invention, there are no special requirements for the composition of the gas to be treated containing acidic gas. In the embodiments of this invention, the advantages of this invention are illustrated by treating associated gas with high hydrogen sulfide content (hydrogen sulfide content of 3600-5000ppm, and other gases including methane and a small amount of carbon dioxide) from Jiangsu oilfield, but this does not limit the scope of this invention.

[0021] In this invention, the liquid-to-gas ratio of the gas to be treated to the alkaline solution can be selected within a wide range. The following is an illustrative description, but it does not limit the scope of the invention. According to a preferred embodiment of the invention, the liquid-to-gas ratio of the gas to be treated to the alkaline solution is 18-28, preferably 19-23. The aforementioned technical solution has advantages such as flexible handling of gas volume changes, complex working conditions, and full applicability to available workspace.

[0022] In this invention, there are no special requirements for the value of the intake air volume Q. The following is an illustrative description, but it does not limit the scope of the invention. According to a preferred embodiment of the invention, Q is 1000-10000m³. 3 / d.

[0023] In this invention, there are no special requirements for the concentration of acidic gas in the gas to be treated. The following is an illustrative description, but it does not limit the scope of the invention. According to a preferred embodiment of the invention, the concentration of acidic gas in the gas to be treated is 500-8000 ppm, preferably 3000-5000 ppm.

[0024] In this invention, the absorption method provided by this invention can absorb and remove various acidic gases. There are no special requirements for the type of acidic gas. The following is an illustrative description, but it does not limit the scope of this invention. According to a preferred embodiment of this invention, the acidic gas is selected from one or more of hydrogen sulfide, carbon dioxide, sulfur dioxide, nitrogen dioxide, and hydrogen chloride, preferably hydrogen sulfide.

[0025] In this invention, there are no special requirements for the type of alkaline solution. The following is an illustrative description, but it does not limit the scope of the invention. According to a preferred embodiment of the invention, the alkaline solution is selected from inorganic alkaline solutions.

[0026] In this invention, there are no special requirements for the type of inorganic base in the inorganic base solution. The following is an illustrative description, but it does not limit the scope of the invention. According to a preferred embodiment of the invention, the inorganic base is selected from one or more of sodium hydroxide, sodium carbonate, and potassium hydroxide.

[0027] In this invention, there are no special requirements for the concentration of the alkaline solution. The following is an illustrative description, but it does not limit the scope of the invention. According to a preferred embodiment of the invention, the concentration of the alkaline solution is 10-15 mg / L.

[0028] In this invention, the alkaline solution circulation rate is the amount of alkaline solution consumed per unit time during the operation of the absorption tower to treat acidic gases.

[0029] In this invention, the circulation rate of the alkaline solution can be selected from a wide range depending on the content and flow rate of the acidic gas in the gas to be treated and the concentration of the alkaline solution. The following is an illustrative description, but it does not limit the scope of the invention. According to a preferred embodiment of the invention, the circulation rate of the alkaline solution is 20-80 m³ / h. 3 / d (i.e., cubic meters per day).

[0030] According to a preferred embodiment of the present invention, the absorption system of the present invention comprises:

[0031] The absorption tower 7, preferably, comprises multiple layers of packed absorption layers, each layer equipped with a thermometer T and a gas sampling port. The gas sampling port is connected to a drying unit, such as a drying column 8. The drying column 8 is connected to an acid gas analyzer 9, which is used to measure the content of unabsorbed acid gas at different locations in the absorption tower and calculate the acid gas absorption rate. The absorption tower is also equipped with a differential pressure gauge 7 for measuring and monitoring the pressure difference between the bottom and top of the absorption tower.

[0032] A gas supply unit is used to supply the required acidic gas to the absorption tower.

[0033] The alkali supply unit is used to supply the required alkali solution to the absorption tower;

[0034] The rich liquor recovery unit is used to recover the rich liquor after absorption by the absorption tower.

[0035] According to a preferred embodiment of the present invention, when the concentration of acidic gas at the gas sampling port of each layer in the absorption tower drops to 0-20 ppm, preferably 0-5 ppm, the gas is discharged from the gas sampling port of each layer in the absorption tower.

[0036] According to a preferred embodiment of the present invention, the packing material of the absorption tower is one or more of plastic Pall ring packing, plastic multifaceted hollow sphere packing, and stainless steel θ ring packing.

[0037] According to a preferred embodiment of the present invention, the porosity of the filler is 0.85-0.97.

[0038] According to one embodiment of the present invention, the gas supply unit preferably includes: a gas storage tank 1 connected in series, a gas mixing tank 2 having a temperature control unit, the gas mixing tank 2 being connected to the acidic gas inlet of the absorption tower, a pressure regulating unit such as an air compressor 3 being installed on the pipeline connecting the gas mixing tank 2 and the acidic gas inlet of the absorption tower for regulating gas pressure, and a gas flow meter such as a precision gas flow meter 4 for monitoring gas flow; and a pressure detector such as a precision pressure gauge 5.

[0039] According to one embodiment of the present invention, the alkali supply unit preferably includes an alkali tank 12 and a metering unit, such as a metering pump 13, wherein the alkali tank 12 is connected to the alkali inlet of the absorption tower through the metering unit.

[0040] According to one embodiment of the present invention, preferably, the alkali inlet of the absorption tower 7 is connected to a shower-type spray unit for spraying alkali into the absorption unit of the absorption tower.

[0041] According to one embodiment of the present invention, the alkaline inlet of the absorption tower 7 is located at the top of the absorption tower;

[0042] According to one embodiment of the present invention, the acidic gas inlet of the absorption tower 7 is located at the bottom of the absorption tower.

[0043] According to one embodiment of the present invention, the exhaust port of the deep absorption tower 7 is located at the top of the absorption tower.

[0044] According to a preferred embodiment of the present invention, the absorption method of the present invention employs the following... Figure 1 The absorption system shown is used for absorption. Gas storage tank 1 includes an acidic gas CO2 storage tank and an inert gas N2 storage tank. First, the acidic gas CO2 storage tank and the inert gas N2 storage tank are connected to a gas mixing tank 2 with a temperature control unit.

[0045] Acidic gases are not limited to CO2, and inert gases are not limited to N2. Acidic gas cylinders, inert gas cylinders, and gas mixing tank 2 are connected by a precision flow control valve. The mixed gas, after passing through a compressor, a precision gas flow meter, and a precision pressure gauge, is introduced into the absorption tower from the bottom, accurately controlling parameters such as the flow rate and pressure of the mixed gas. The temperature of gas mixing tank 2 is 20-40℃, the pressure is 0.05MPa-0.15MPa, and the discharge gas volume is 1000-10000 m³ / h. 3 / d.

[0046] The mixed gas enters the bottom of the absorption tower from the gas mixing tank 2, and is equipped with an air compressor 3, a precision gas flow meter 4, and a precision pressure gauge 5 to control parameters such as gas pressure and flow rate.

[0047] like Figure 1As shown, the absorption tower 7 is equipped with multiple layers of packing chambers to increase the contact area between acidic gas and alkaline solution. Each packing chamber is equipped with a thermometer 10 and a gas sampling port. The sampling port is connected to an acidic gas analyzer 9 after passing through a drying column 8 to measure the content of unabsorbed acidic gas at different locations in the absorption tower and calculate the acidic gas absorption rate. A differential pressure gauge 11 is also installed to monitor the pressure difference between the bottom and top of the absorption tower.

[0048] According to a preferred embodiment of the present invention, the inlet gas flow rate in the absorption tower is 1000-10000 m / s. 3 / d.

[0049] According to a preferred embodiment of the present invention, the temperature of the inlet gas in the absorption tower is 25-50°C.

[0050] According to a preferred embodiment of the present invention, the inlet gas pressure in the absorption tower is 0.04-0.5 MPa.

[0051] like Figure 1 As shown, the alkaline solution is pumped to the top of the absorption tower by metering pump 13, sprayed from top to bottom, and fully contacts the gas in the packing chamber. The rich solution after absorbing the acidic gas is recycled into the rich solution tank 6. The alkaline solution tank 12 and the rich solution tank 6 are equipped with pH meters to monitor the acidity and alkalinity of the solution.

[0052] The absorption method described in this invention is particularly suitable for the removal of hydrogen sulfide in oil and gas fields.

[0053] The present invention will be described in detail below through embodiments.

[0054] In the following embodiments,

[0055] Parameters such as pressure, temperature, liquid / gas flow rate, and pH are measured by the device's monitoring instruments;

[0056] The hydrogen sulfide content in the gas to be treated and the hydrogen sulfide content in the exhaust gas after treatment were obtained by analyzing gas samples taken at multiple different times of the day using a portable gas analyzer and taking the average value.

[0057] The gas-liquid ratio is the ratio of the alkaline solution circulation rate (L / d) to the gas intake rate (m³ / d). 3 / d) ratio;

[0058] In this embodiment of the invention, the absorber packing is a commercially available plastic Pall ring packing;

[0059] In this embodiment of the invention, the gas to be treated is associated gas with high hydrogen sulfide content from Jiangsu Oilfield, and the gas composition is hydrogen sulfide, methane and a small amount of carbon dioxide.

[0060] Example 1

[0061] according to Figure 1The process shown is carried out in a two-tower series configuration, with gas and alkali solution fed into the first tower.

[0062] The hydrogen sulfide content in the gas to be treated is 3800 ppm, the outlet temperature of the gas mixing tank is 28℃, the outlet pressure is 0.11 MPa, the alkaline solution is sodium hydroxide solution (12 mg / L), and the liquid-to-gas ratio is 19.

[0063] The porosity of the packing material inside each absorption tower is 0.95;

[0064] The total gas intake volume Q is 1440 m³. 3 / d, M is 0.31, N is 0.0000754, a is 3.9, b is 0.000554, k is 1.1, the diameter D of the first and second absorption towers is 0.46m, the packing height H is 5.16m, and the circulation rate of sodium hydroxide solution is 27m³. 3 / d.

[0065] Results: The hydrogen sulfide content in the treated exhaust gas was 2 ppm.

[0066] Example 2

[0067] according to Figure 1 The process shown is performed using a single-tower mode;

[0068] The hydrogen sulfide content in the gas to be treated is 5000 ppm, the outlet temperature of the gas mixing tank is 28℃, the outlet pressure is 0.08 MPa, and the flow rate of the acidic gas is 2800 m / s. 3 / d, the alkaline solution is sodium hydroxide solution (10mg / L), and the liquid-to-gas ratio is 23;

[0069] The porosity of the packing material inside the absorption tower is 0.95;

[0070] The intake volume Q is 2800m³ 3 / d, M is 0.36, N is 0.0000893, a is 5.19, b is 0.000608, k is 1.2, the absorption tower diameter D is 0.73m, the packing height H is 8.27m, and the sodium hydroxide solution circulation rate is 64.4m³. 3 / d.

[0071] Results: The hydrogen sulfide content in the treated exhaust gas was 4 ppm.

[0072] Example 3

[0073] according to Figure 1 The process shown is carried out in a two-tower parallel mode, with the two towers having the same throughput, that is, the gas and alkali solution are divided into two equal streams and fed into the two towers respectively.

[0074] The hydrogen sulfide content in the gas to be treated is 3800 ppm, the outlet temperature of the gas mixing tank is 28℃, the outlet pressure is 0.12 MPa, the alkaline solution is sodium hydroxide solution (10 mg / L), and the liquid-to-gas ratio is 19.

[0075] The porosity of the packing material inside each absorption tower is 0.95;

[0076] The total intake volume Q is 1200m³. 3 / d, M is 0.33, N is 0.0000921, a is 2.51, b is 0.000617, k is 1.1, the diameter D of each absorption tower is 0.48m, the packing height H is 3.58m, and the circulation rate of sodium hydroxide solution is 22.8m. 3 / d.

[0077] Results: The hydrogen sulfide content in the treated exhaust gas was 3 ppm.

[0078] Example 4

[0079] according to Figure 1 The process shown is carried out using a three-tower series configuration, with material fed from the first tower.

[0080] The hydrogen sulfide content in the gas to be treated is 3800 ppm, the outlet temperature of the gas mixing tank is 28℃, the outlet pressure is 0.06 MPa, the alkaline solution is sodium hydroxide solution (10 mg / L), and the liquid-to-gas ratio is 19.

[0081] The porosity of the packing material inside the absorption tower is 0.95;

[0082] The total intake volume Q is 2000m³. 3 / d, M is 0.23, N is 0.0000573, a is 2.84, b is 0.000454, k is 1.1, the diameter D of each absorption tower is 0.38m, the packing height H is 4.12m, and the circulation rate of sodium hydroxide solution is 38m³. 3 / d.

[0083] Results: The hydrogen sulfide content in the treated exhaust gas was 2 ppm.

[0084] Example 5

[0085] according to Figure 1 The process shown is carried out in a four-tower mode, with two towers connected in series as a group and then connected in parallel. The two parallel units have the same processing capacity and both are fed from the first tower.

[0086] The hydrogen sulfide content in the gas to be treated is 4000ppm, the outlet temperature of the gas mixing tank is 28℃, the outlet pressure is 0.25MPa, the alkaline solution is sodium hydroxide solution (10mg / L), and the liquid-to-gas ratio is 19.

[0087] The porosity of the packing material inside the absorption tower is 0.95;

[0088] The total intake volume Q is 3000m³. 3 / d, M is 0.17, N is 0.0000372, a is 2.046, b is 0.000291, k is 1.2, the diameter D of each absorption tower is 0.35m, the packing height H is 3.5m, and the circulation rate of sodium hydroxide solution is 57m³. 3 / d.

[0089] Results: The hydrogen sulfide content in the treated exhaust gas was 5 ppm.

[0090] Example 6

[0091] The method is the same as in Example 2, except that M is 0.3, N is 0.0000552, a is 4.8, b is 0.000623, k is 1.1, the absorption tower diameter D is 0.5m, the packing height H is 7.2m, and the circulation rate of the sodium hydroxide solution is 64.4m³. 3 / d.

[0092] Results: The average hydrogen sulfide content in the treated exhaust gas was 15 ppm.

[0093] Example 7

[0094] The method is the same as in Example 1, except that M is 0.35, N is 0.0000775, a is 4.1, b is 0.000625, k is 1.3, the diameter D of the first and second absorption towers is 0.6m, the packing height H is 6.5m, and the sodium hydroxide circulation rate is 26.6m. 3 / d.

[0095] Results: The hydrogen sulfide content in the treated exhaust gas was 20 ppm.

[0096] Example 8

[0097] The method is the same as in Example 3, except that M is 0.36, N is 0.0000636, a is 3.8, b is 0.00024, k is 1.1, the diameter D of each absorption tower is 0.48m, the packing height H is 4.5m, and the circulation rate of sodium hydroxide solution is 22.8m. 3 / d.

[0098] Results: The hydrogen sulfide content in the treated exhaust gas was 15 ppm.

[0099] Comparative Example 1

[0100] according to Figure 1 The process shown is performed using a single-tower mode;

[0101] The hydrogen sulfide content in the gas to be treated is 5000 ppm, the outlet temperature of the gas mixing tank is 28℃, the outlet pressure is 0.08 MPa, and the flow rate of the acidic gas is 2800 m / s. 3 / d, the alkaline solution is sodium hydroxide solution (10mg / L), and the liquid-to-gas ratio is 23;

[0102] The porosity of the packing material inside the absorption tower is 0.95;

[0103] The intake volume Q is 2800m³ 3 The absorption tower has a diameter D of 0.34 m, a packing height H of 10.8 m, and a sodium hydroxide solution circulation rate of 64.4 m³ / d. 3 / d.

[0104] Results: The average hydrogen sulfide content in the treated exhaust gas was 55 ppm.

[0105] Comparative Example 2

[0106] according to Figure 1 The process shown is carried out using a two-tower series configuration, with material fed from the first tower.

[0107] The hydrogen sulfide content in the gas to be treated is 3800 ppm, the outlet temperature of the gas mixing tank is 28℃, the outlet pressure is 0.11 MPa, and the flow rate of the acidic gas is 1440 m / s. 3 / d, the alkaline solution is sodium hydroxide solution (12mg / L), and the liquid-to-gas ratio is 19;

[0108] The porosity of the packing material inside each absorption tower is 0.95;

[0109] The gas intake flow rate Q is 1440 m³. 3 / d, the diameter D of the first and second absorption towers is 0.41m, and the packing height H is 9.5m; the sodium hydroxide circulation rate is 26.6m. 3 / d.

[0110] Results: The hydrogen sulfide content in the treated exhaust gas was 75 ppm.

[0111] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A method for absorbing acidic gases, characterized in that, The method includes: contacting the gas to be treated, containing acidic gas, with an alkaline solution in an absorption tower; designing the absorption towers according to the number and connection method of the absorption towers and the inlet flow rate of the gas to be treated, ensuring that the design meets the following requirements: Q is based on m 3 / d represents the unit of gas intake volume; D represents the diameter of the absorption tower in meters; H represents the height of the absorption tower packing in meters; and k ranges from 1.1 to 1.

3. The diameter D and packing height H of the absorption tower satisfy the following conditions: D = (M + N * Q) * k; M is 0.1-0.4; N is 0.00005-0.0001; H = (a + b * Q) * k; a is 2 - 6; b is 0.0002 - 0.0008.

2. The absorption method according to claim 1, wherein, The absorption tower is a single-tower design, and its diameter and packing height satisfy: D = (0.36 + 0.0000893 * Q) * k; H = (5.19 + 0.000608 * Q) * k; and / or The absorption towers are configured as two towers connected in series. The diameter and packing height of each absorption tower satisfy the following conditions: D = (0.31 + 0.0000754 × Q) * k; H = (3.9 + 0.000554 × Q) * k; preferably, the gas to be treated containing acidic gas and the alkaline solution are fed from the first tower; and / or The absorption towers are configured as two towers connected in parallel. The diameter and packing height of each absorption tower satisfy the following conditions: D = (0.33 + 0.0000921 * Q) * k; H = (2.51 + 0.000617 * Q) * k. Preferably, the ratio of the throughput of the first tower to the second tower is 0.1-10:1, more preferably the throughput of the first tower and the second tower are the same; and / or The absorption towers are arranged in a three-tower series configuration, with the diameter and packing height of each tower satisfying the following conditions: D = (0.23 + 0.0000573 * Q) * k; H = (2.84 + 0.000454 * Q) * k. Preferably, the gas to be treated containing acidic gas and the alkaline solution are fed from the first tower; and / or The absorption tower is a four-tower configuration, in which two towers are connected in series as a group and then in parallel. The diameter and packing height of each absorption tower satisfy the following conditions: D = (0.17 + 0.0000372 * Q) * k; H = (2.046 + 0.000291 * Q) * k. Preferably, the ratio of the processing capacity of each parallel unit is 0.1-10:1, and each parallel unit is fed from the first tower. More preferably, the processing capacity of each parallel unit is the same.

3. The absorption method according to claim 1 or 2, wherein, The liquid-to-gas ratio of the alkaline solution to the gas to be treated is 18-28, preferably 19-23.

4. The absorption method according to any one of claims 1-3, wherein, Q is 1000-10000m 3 / d; and / or The concentration of acidic gas in the gas to be treated is 500-8000 ppm, preferably 3000-5000 ppm.

5. The absorption method according to any one of claims 1-4, wherein, The acidic gas is selected from one or more of hydrogen sulfide, carbon dioxide, sulfur dioxide, nitrogen dioxide, and hydrogen chloride, with hydrogen sulfide being preferred.

6. The absorption method according to any one of claims 1-5, wherein, The alkaline solution is selected from inorganic alkaline solutions; Preferably, the inorganic base is selected from one or more of sodium hydroxide, sodium carbonate, and potassium hydroxide; and / or The concentration of the alkaline solution is 10-15 mg / L; and / or The circulation volume of the alkaline solution is 20-80 m³. 3 / d.

7. The absorption method according to any one of claims 1-6, wherein, Each of the aforementioned absorption towers is provided with multiple layers of absorption packing chambers, and each packing chamber is equipped with a thermometer and a gas sampling port; and / or After absorption by the absorption tower, the concentration of acidic gas in the discharged gas is 0-20 ppm, preferably 0-5 ppm.

8. The absorption method according to any one of claims 1-7, wherein, The packing material of each of the absorption towers is one or more of the following: plastic Pall ring packing, plastic multifaceted hollow sphere packing, and stainless steel θ-ring packing; and / or The porosity of the filler is 0.85-0.

97.

9. The absorption method according to any one of claims 1-8, wherein, The operating conditions for each of the aforementioned absorption towers include: The intake gas velocity is 1000-10000m. 3 / d; and / or The intake gas temperature is 25-50℃; and / or The intake gas pressure is 0.04-0.5 MPa.

10. The application of the absorption method according to any one of claims 1-9 in the removal of hydrogen sulfide in oil and gas fields.

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