A concentration device, a concentration method, and a production system for acetylene produced by partial oxidation of hydrocarbons

Abstract

The application discloses a concentration device for acetylene prepared by partial oxidation of hydrocarbons, which comprises a countercurrent desorption tower, a desorbent inlet is arranged at the bottom of the countercurrent desorption tower, a carrier solvent inlet and a circulating gas outlet are arranged at the top of the countercurrent desorption tower, and an acetylene collection outlet is arranged at the middle of the countercurrent desorption tower, the acetylene collection outlet divides the countercurrent desorption tower into an upper tower section and a lower tower section, and the height H1 of the upper tower section, the annual acetylene processing capacity T of the tower and the tower diameter D1 of the upper tower section satisfy the value of H1*T / D1 2 between 18 and 35, the height H2 of the lower tower section, the annual acetylene processing capacity T of the tower and the tower diameter D2 of the lower tower section satisfy the value of H2*T / D2 2 between 18 and 38, the tower diameter D2 is always not less than the tower diameter D1, the height of the lower tower section is always not less than the height of the upper tower section, and the height proportion of the fillers or tower trays in the interior of the upper tower section and the lower tower section is not less than 70%. The scheme solves the problem of how to further improve the acetylene purity collected by the countercurrent desorption tower in the prior art.

Description

Technical Field

[0001] This invention relates to the concentration of acetylene, specifically to a concentration apparatus, concentration method, and production system for the partial oxidation of hydrocarbons to produce acetylene. Background Technology

[0002] Acetylene is a very important organic chemical raw material, widely used in metal processing, welding, cutting, and the preparation of chemical products such as vinyl chloride, trichloroethylene, vinyl acetate, acrylonitrile, and 1,4-butanediol. The main methods for preparing acetylene include non-catalytic partial oxidation of hydrocarbons, electric arc oxidation, and plasma oxidation, or wet or dry methods using calcium carbide as a raw material. This invention primarily focuses on a process apparatus for the concentration and refining of acetylene produced from hydrocarbons, especially natural gas, through non-catalytic partial oxidation.

[0003] In the existing technology, the main structure and main production process of the production equipment used in the non-catalytic partial oxidation of hydrocarbons to acetylene are as follows: the hydrocarbon pipeline and the oxygen pipeline are first connected to the gas heater. Natural gas and oxygen are preheated to 500-650℃ respectively and then introduced into the acetylene reactor. After being fully mixed, they enter the reaction chamber of the acetylene furnace. Since the amount of oxygen introduced is insufficient to completely oxidize the natural gas, the reaction gas composed of natural gas and oxygen only undergoes a partial oxidation reaction in the acetylene furnace reaction chamber. The remaining natural gas undergoes a cracking reaction. After a few milliseconds of reaction, it is rapidly quenched to end the reaction. The hydrocarbon is partially oxidized and cracked into a cracked gas mixture containing components such as acetylene, carbon monoxide, carbon dioxide, hydrogen, butadiyne, aromatic hydrocarbons, and carbon black. The cracked gas mixture from the acetylene reactor then passes through the lower section of the cooling tower, the electrostatic precipitator, and the upper section of the cooling tower. After further cooling and washing away the carbon black, it enters the enrichment system through the compressor to obtain the product acetylene and syngas, as well as the by-product high alkyne gas stream.

[0004] The concentration unit refines cracked gas from the partial oxidation unit using N-methylpyrrolidone (NMP) and other solvents through pressurized absorption and atmospheric desorption. Because the cracked gas contains aromatic hydrocarbons such as naphthalene, which are prone to polymerization and crystallization that can clog the system, the cracked gas from the compressor first enters a pre-washing tower to remove easily soluble contaminants such as naphthalene. The solvent at the bottom of the pre-washing tower enters an acetylene stripping tower and, after depressurization, recovers acetylene using syngas stripping; naphthalene and other substances remain in the solution. The gas at the top of the tower is recovered and recycled to the inlet of the cracked gas compressor. The solvent at the bottom of the tower enters an advanced alkyne stripping tower where NMP containing dissolved substances is desorbed under reduced pressure to remove advanced alkynes.

[0005] The cracked gas, after being washed in the pre-washing tower, enters the main washing tower. Acetylene and more soluble components in the cracked gas dissolve in NMP, while components less soluble than acetylene are treated as tail gas, i.e., syngas, and exited at the top of the tower. The NMP containing dissolved substances from the main washing tower enters the countercurrent desorption tower, where atmospheric pressure desorption occurs under the action of packing material or trays. At the top of the countercurrent desorption tower, carbon dioxide-rich acetylene gas is desorbed and returned to the inlet of the cracked gas compressor for recycling. A product acetylene stream is collected from the side stream in the middle of the desorption tower, completing the acetylene enrichment process in the cracked gas.

[0006] Chinese patent document CN106431814A discloses a process and apparatus for acetylene concentration, wherein the acetylene concentration apparatus includes a pre-absorption tower, a main absorption tower, a desorption tower, a compressor I, and a compressor II. The top of the pre-absorption tower is connected to the bottom of the main absorption tower, the bottom of the main absorption tower is connected to the top of the desorption tower, the compressor I is connected to the bottom of the pre-absorption tower, and the compressor II is located between the pre-absorption tower and the main absorption tower. The process for acetylene concentration includes the following steps: 1) A mixed gas containing acetylene is introduced into compressor I for the first compression and pressurization; 2) The compressed mixed gas enters the bottom of the pre-absorption tower and comes into countercurrent contact with solvent I from the top of the tower, removing most of the higher alkynes, some acetylene, and a small amount of sparingly soluble gases from the mixed gas; 3) The mixed gas absorbed by solvent I enters compressor II from the top of the pre-absorption tower for the second compression and pressurization; 4) The mixed gas after the second compression enters the bottom of the main absorption tower and comes into countercurrent contact with solvent II from the top of the tower, where most of the acetylene and the remaining higher alkynes in the mixed gas are absorbed by solvent II, and the insoluble gases are discharged from the top of the tower; 5) Solvent II, which absorbs acetylene, is introduced into a desorption tower for desorption, and the acetylene product is produced from the middle of the desorption tower, while the desorbed gas is discharged from the top of the desorption tower. The existing technology employs a segmented pressurization method, which can improve the purity and yield of acetylene, reduce the content of higher alkynes such as propadiene in the product, prevent waste and pollution from reprocessing concentrated sulfuric acid, and simultaneously reduce the amount of absorbent used in the absorption process, thus lowering the energy consumption of the entire concentration process, achieving multiple benefits. However, this existing technology does not address how to further reduce the impurity content of the acetylene extracted from the desorption tower, thereby further improving the acetylene purity.

[0007] Chinese patent document CN219002005U discloses an acetylene flash desorption device for acetylene concentration, comprising a first-stage flash evaporator, a second-stage flash evaporator, and a third-stage flash evaporator connected in series from top to bottom; the gas outlets of the first-stage, second-stage, and third-stage flash evaporators are respectively connected to a desorption tower; the desorption tower includes a first gas outlet and a second gas outlet; the first gas outlet is located at the top of the desorption tower; the second gas outlet is located in the middle of the desorption tower body. This prior art divides the flash tower into three flash evaporators connected in series. The cracked gas used to prepare acetylene is sequentially flash-separated into different components in the three flash evaporators. These different components enter different sections of the desorption tower, are further desorbed, and are collected from different outlets of the desorption tower. High-purity gas can be obtained from the gas outlet of the tower body.

[0008] Chinese patent document CN109796295A discloses a natural gas cracking acetylene enrichment system and its process. The system includes a pre-washing tower, a main washing tower, an acetylene stripping tower, a tail gas scrubbing tower, a countercurrent desorption tower, and a solvent treatment unit. The solvent treatment unit includes a potassium carbonate addition device, a thermal desorption tower, a vacuum tower, and a high-grade acetylene stripping tower. The pre-washing tower is connected to the main washing tower and the acetylene stripping tower, respectively. The main washing tower is connected to the tail gas scrubbing tower and the countercurrent desorption tower. The countercurrent desorption tower outputs circulating gas and acetylene gas. The process steps are as follows: (1) The cracked gas enters the pre-washing tower, and NMP solvent is added to the pre-washing tower to remove most of the higher alkynes. Then, it is sent to the main washing tower. (2) NMP solvent is added to the main washing tower to separate the acetylene and the synthesis gas. The synthesis gas enters the tail gas washing tower and is washed with condensate. The acetylene-rich solvent enters the countercurrent desorption tower. (3) The acetylene-rich solvent desorbs the acetylene and the circulating gas in the countercurrent desorption tower. The remaining solution is sent to the solvent treatment unit. (4) Potassium carbonate solution is added to the remaining solution. Then, it passes through the thermal desorption tower to desorb a small amount of acetylene and return it to the countercurrent desorption tower. The solution is input to the vacuum tower. (5) The acetylene is further desorbed in the vacuum tower. The acetylene gas is sent to the thermal desorption tower, and the remaining solution is sent to the higher alkyne stripping tower. (6) The higher alkyne is removed in the higher alkyne stripping tower, and the solvent is recovered. The advantages of this prior art are: the addition of potassium carbonate to the system effectively reduces corrosion inside the concentration unit; the added potassium carbonate solution inhibits polymer formation and reduces system blockage; the unit operates smoothly, reducing NMP solvent consumption, extending the equipment cleaning and maintenance cycle, and thus lowering production costs. However, this prior art still does not disclose how to further improve the purity of the acetylene extracted from the desorption tower. Summary of the Invention

[0009] The purpose of this invention is to provide a concentration device, concentration method, and production system for the partial oxidation of hydrocarbons to produce acetylene, in order to solve the problem of how to further improve the purity of acetylene extracted from countercurrent desorption towers in the prior art.

[0010] To achieve the above objectives, the basic embodiment of the present invention provides a concentration device for the partial oxidation of hydrocarbons to acetylene, comprising a countercurrent desorption tower. The bottom of the countercurrent desorption tower has a desorbent inlet, the top of the countercurrent desorption tower has a carrier solvent inlet and a circulating gas outlet, and the middle of the countercurrent desorption tower has an acetylene collection outlet. The acetylene collection outlet divides the countercurrent desorption tower into an upper section and a lower section. The height H1 of the upper section, the annual acetylene throughput T of the tower, and the diameter D1 of the upper section satisfy H1×T / D1. 2 The value is between 18 and 35, and the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is between 18 and 38, and the tower diameter D2 is always not less than the tower diameter D1. The height of the lower section of the tower is always not less than the height of the upper section of the tower. The height of the packing or tray inside the upper and lower sections of the tower is not less than 70%.

[0011] Preferably, to further improve the purity of the acetylene extracted from the desorption tower, the height H1 of the upper section of the tower, the annual acetylene throughput T of the tower, and the diameter D1 of the upper section of the tower satisfy the relationship H1×T / D1. 2 The value is between 23 and 31. Further preferred values ​​are 26, 27, or 28.

[0012] Preferably, to further improve the purity of the acetylene extracted from the desorption tower, the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is between 23 and 33. Further preferred values ​​are 27, 28, or 29.

[0013] Preferably, to further improve the purity of the acetylene collected from the desorption tower, the height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy a value of H2 / (H1+H2) between 0.6 and 0.63. A further preferred value is 0.61 or 0.62.

[0014] Secondly, the present invention provides a method for concentrating acetylene through partial oxidation of hydrocarbons, comprising: performing acetylene concentration operation using any of the concentration devices described above, wherein the ratio of the gas flow rate from the top of the countercurrent desorption tower is 0.5-1. This configuration is advantageous for further improving the purity of the acetylene extracted from the desorption tower.

[0015] Preferably, in order to further improve the purity of the acetylene extracted from the desorption tower, the top gas flow rate ratio of the countercurrent desorption tower is 0.7 or 0.8.

[0016] Thirdly, the present invention provides a production system for the partial oxidation of hydrocarbons to produce acetylene, including any of the concentration devices described above.

[0017] The present invention has the following beneficial effects:

[0018] This invention improves the structure of the countercurrent desorption tower, thereby further reducing the content of impurities (such as propadiene and carbon dioxide) in the acetylene gas collected from the tower and improving its purity. Through trial use, this invention can reduce the impurity content in the acetylene gas stream collected from the countercurrent desorption tower by 15%-30%. The effectiveness of this invention is achieved through structural improvements to the countercurrent desorption tower, requiring only a one-time investment. Compared to the continuous investment methods of existing technologies that involve pressurization or material addition, this invention offers advantages such as simple implementation and low cost. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of an embodiment of a hydrocarbon partial oxidation to acetylene enrichment device, enrichment method, and production system according to the present invention. Detailed Implementation

[0020] In this invention, the annual acetylene processing capacity T of the tower is a value in units of 10,000 tons. The units for tower height and tower diameter are both meters, the international unit of length.

[0021] The height H1 of the upper section of the tower, the annual acetylene throughput T of the tower, and the diameter D1 of the upper section of the tower satisfy the relationship H1×T / D1. 2 The value is between 18 and 35, for example, it can be 19, 20, 21, 22, 23, 24, 25, 26, 27, 28, 29, 30, 31, 32, 33, 34, etc.

[0022] The height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is between 18 and 38, for example, it can be 19, 20, 21, 22, 23, 24, 25, 26, 27, 28, 29, 30, 31, 32, 33, 34, 35, 36, 37, etc.

[0023] The top gas flow rate ratio refers to the ratio of the volume of gas extracted from the top of the tower to the volume of gas at the acetylene collection outlet per unit time.

[0024] The top gas flow rate ratio of the countercurrent desorption tower is 0.5-1, for example, it can be 0.6, 0.7, 0.8, 0.9, etc.

[0025] The packing or tray height ratio inside the upper and lower sections of the tower shall not be less than 70%, such as 75%, 80%, 85%, 90%, etc.

[0026] The following detailed description illustrates the specific implementation method:

[0027] The reference numerals in the accompanying drawings include: 1. Circulating gas outlet; 2. Carrier solvent inlet; 3. Upper section of the tower; 4. Lower section of the tower; 5. Desorbent inlet; 6. Acetylene collection outlet.

[0028] Example 1: Basic as shown in the attached document Figure 1 The diagram shows a hydrocarbon partial oxidation to acetylene enrichment device, comprising a countercurrent desorption tower. The bottom of the countercurrent desorption tower has a desorbent inlet, the top has a carrier solvent inlet and a recirculating gas outlet, and the middle section has an acetylene collection outlet, dividing the countercurrent desorption tower into an upper section and a lower section. The height H1 of the upper section, the annual acetylene throughput T, and the diameter D1 of the upper section satisfy H1×T / D1. 2 The value is 27, and the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is 28. In this embodiment, the height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy the condition that H2 / (H1+H2) is 0.61. In this embodiment, the packing or tray height in the upper section of the tower accounts for 70% of the total height, and the packing or tray height in the lower section of the tower accounts for 70% of the total height. In this embodiment, the liquid distributor in the countercurrent desorption tower is preferably a tray-type liquid distributor.

[0029] Example 2: Basic as attached Figure 1 The diagram shows a hydrocarbon partial oxidation to acetylene enrichment device, comprising a countercurrent desorption tower. The bottom of the countercurrent desorption tower has a desorbent inlet, the top has a carrier solvent inlet and a recirculating gas outlet, and the middle section has an acetylene collection outlet, dividing the countercurrent desorption tower into an upper section and a lower section. The height H1 of the upper section, the annual acetylene throughput T, and the diameter D1 of the upper section satisfy H1×T / D1. 2 The value is 27, and the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2The value is 28. In this embodiment, the height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy the condition that H2 / (H1+H2) is 0.62. In this embodiment, the packing or tray height in the upper section of the tower accounts for 70% of the total height, and the packing or tray height in the lower section of the tower accounts for 70% of the total height. In this embodiment, the liquid distributor in the countercurrent desorption tower is preferably a tray-type liquid distributor.

[0030] Example 3: Basically as shown in the attached document Figure 1 The diagram shows a hydrocarbon partial oxidation to acetylene enrichment device, comprising a countercurrent desorption tower. The bottom of the countercurrent desorption tower has a desorbent inlet, the top has a carrier solvent inlet and a recirculating gas outlet, and the middle section has an acetylene collection outlet, dividing the countercurrent desorption tower into an upper section and a lower section. The height H1 of the upper section, the annual acetylene throughput T, and the diameter D1 of the upper section satisfy H1×T / D1. 2 The value is 19, and the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is 20. In this embodiment, the height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy the condition that H2 / (H1+H2) is 0.61. In this embodiment, the packing or tray height in the upper section of the tower accounts for 70% of the total height, and the packing or tray height in the lower section of the tower accounts for 70% of the total height. In this embodiment, the liquid distributor in the countercurrent desorption tower is preferably a tray-type liquid distributor.

[0031] Example 4: Basic as attached Figure 1 The diagram shows a hydrocarbon partial oxidation to acetylene enrichment device, comprising a countercurrent desorption tower. The bottom of the countercurrent desorption tower has a desorbent inlet, the top has a carrier solvent inlet and a recirculating gas outlet, and the middle section has an acetylene collection outlet, dividing the countercurrent desorption tower into an upper section and a lower section. The height H1 of the upper section, the annual acetylene throughput T, and the diameter D1 of the upper section satisfy H1×T / D1. 2 The value is 34, and the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is 37. In this embodiment, the height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy the condition that H2 / (H1+H2) is 0.61. In this embodiment, the packing or tray height in the upper section of the tower accounts for 70% of the total height, and the packing or tray height in the lower section of the tower accounts for 70% of the total height. In this embodiment, the liquid distributor in the countercurrent desorption tower is preferably a tray-type liquid distributor.

[0032] Example 5: Basic as attached Figure 1The diagram shows a hydrocarbon partial oxidation to acetylene enrichment device, comprising a countercurrent desorption tower. The bottom of the countercurrent desorption tower has a desorbent inlet, the top has a carrier solvent inlet and a recirculating gas outlet, and the middle section has an acetylene collection outlet, dividing the countercurrent desorption tower into an upper section and a lower section. The height H1 of the upper section, the annual acetylene throughput T, and the diameter D1 of the upper section satisfy H1×T / D1. 2 The value is 34, and the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is 37. In this embodiment, the height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy the condition that H2 / (H1+H2) is 0.62. In this embodiment, the packing or tray height in the upper section of the tower accounts for 70% of the total height, and the packing or tray height in the lower section of the tower accounts for 70% of the total height. In this embodiment, the liquid distributor in the countercurrent desorption tower is preferably a tray-type liquid distributor.

[0033] Example 6: A method for concentrating acetylene by partial oxidation of hydrocarbons, comprising using the concentration device in Example 1 to perform acetylene concentration operation, wherein the flow rate ratio of the gas collected at the top of the countercurrent desorption tower is 0.5.

[0034] Example 7: A method for concentrating acetylene by partial oxidation of hydrocarbons, comprising using the concentration device in Example 2 to perform acetylene concentration operation, wherein the flow rate ratio of the gas collected at the top of the countercurrent desorption tower is 0.6.

[0035] Example 8: A method for concentrating acetylene by partial oxidation of hydrocarbons, comprising using the concentration apparatus in Example 3 for acetylene concentration operation, wherein the flow rate ratio of the gas collected at the top of the countercurrent desorption tower is 0.9.

[0036] Example 9: A method for concentrating acetylene by partial oxidation of hydrocarbons, comprising using the concentration apparatus in Example 4 to perform acetylene concentration operation, wherein the flow rate ratio of the gas collected at the top of the countercurrent desorption tower is 0.7.

[0037] Comparative Example 1: A method for concentrating acetylene through partial oxidation of hydrocarbons, comprising using a concentration device for acetylene concentration. The concentration device includes a countercurrent desorption tower, with a desorbent inlet at the bottom, a carrier solvent inlet and a recirculating gas outlet at the top, and an acetylene collection outlet in the middle, dividing the countercurrent desorption tower into an upper section and a lower section. The height H1 of the upper section, the annual acetylene throughput T, and the tower diameter D1 of the upper section satisfy H1×T / D1. 2 The value is 16, and the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2.2 The value is 18. In this comparative example, the height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy the condition that H2 / (H1+H2) is 0.6. In this comparative example, the liquid distributor in the countercurrent desorption tower is preferably a sieve plate type liquid distributor. During the concentration operation, the flow rate ratio of the gas collected at the top of the countercurrent desorption tower is 1.

[0038] Comparative Example 2: A method for concentrating acetylene through partial oxidation of hydrocarbons, comprising using a concentration device for acetylene concentration. The concentration device includes a countercurrent desorption tower, with a desorbent inlet at the bottom, a carrier solvent inlet and a recirculating gas outlet at the top, and an acetylene collection outlet in the middle, dividing the countercurrent desorption tower into an upper section and a lower section. The height H1 of the upper section, the annual acetylene throughput T, and the tower diameter D1 of the upper section satisfy H1×T / D1. 2 The value is 36, and the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is 39. In this comparative example, the height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy the condition that H2 / (H1+H2) is 0.64. In this comparative example, the liquid distributor in the countercurrent desorption tower is preferably a sieve plate type liquid distributor. During the concentration operation, the ratio of the gas flow rate from the top of the countercurrent desorption tower to the total height of the tower is 0.4.

[0039] Example 10: The present invention provides a production system for the partial oxidation of hydrocarbons to produce acetylene, including any one of the concentration devices in Examples 1 to 5 above.

[0040] The acetylene concentration data for Examples 6, 7, 8, and 9, and Comparative Examples 1 and 2 are shown in the table below:

[0041]

[0042] The above descriptions are merely embodiments of the present invention, and common knowledge regarding specific structures and characteristics in the solutions is not described in detail here. It should be noted that those skilled in the art can make various modifications and improvements without departing from the structure of the present invention, and these should also be considered within the scope of protection of the present invention. These modifications and improvements will not affect the effectiveness of the implementation of the present invention or the practicality of the patent.

Claims

1. A concentration device for the partial oxidation of hydrocarbons to acetylene, comprising a countercurrent desorption tower, wherein a desorbent inlet is provided at the bottom of the countercurrent desorption tower, a carrier solvent inlet and a circulating gas outlet are provided at the top of the countercurrent desorption tower, and an acetylene collection outlet is provided in the middle of the countercurrent desorption tower, the acetylene collection outlet dividing the countercurrent desorption tower into an upper section and a lower section, characterized in that: The height H1 of the upper section of the tower, the annual acetylene throughput T of the tower, and the diameter D1 of the upper section of the tower satisfy the relationship H1×T / D1. 2 The value is between 18 and 35, and the height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is between 18 and 38, and the tower diameter D2 is always not less than the tower diameter D1. The height of the lower section of the tower is always not less than the height of the upper section of the tower. The height of the packing or tray inside the upper and lower sections of the tower is not less than 70%.

2. The concentrator for the partial oxidation of hydrocarbons to acetylene according to claim 1, characterized in that: The height H1 of the upper section of the tower, the annual acetylene throughput T of the tower, and the diameter D1 of the upper section of the tower satisfy the relationship H1×T / D1. 2 The value is between 23 and 31.

3. The concentrator for the partial oxidation of hydrocarbons to acetylene according to claim 2, characterized in that: The height H1 of the upper section of the tower, the annual acetylene throughput T of the tower, and the diameter D1 of the upper section of the tower satisfy the relationship H1×T / D1. 2 The value is 26, 27 or 28.

4. The concentrator for the partial oxidation of hydrocarbons to acetylene according to claim 3, characterized in that: The height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is between 23 and 33.

5. The concentrator for the partial oxidation of hydrocarbons to acetylene according to claim 4, characterized in that: The height H2 of the lower section of the tower, the annual acetylene throughput T of the tower, and the diameter D2 of the lower section of the tower satisfy the relationship H2×T / D2. 2 The value is 27, 28 or 29.

6. A concentration apparatus for the partial oxidation of hydrocarbons to acetylene according to any one of claims 1-5, characterized in that: The height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy the condition that the value of H2 / (H1+H2) is between 0.6 and 0.

63.

7. The concentrator for the partial oxidation of hydrocarbons to acetylene according to claim 6, characterized in that: The height H2 of the acetylene collection outlet and the total height of the countercurrent desorption tower satisfy the condition that the value of H2 / (H1+H2) is 0.61 or 0.

62.

8. The method for concentrating acetylene by partial oxidation of hydrocarbons according to claim 7, characterized in that: Acetylene enrichment is performed using the enrichment device described in any one of claims 1-7, wherein the ratio of the gas flow rate from the top of the countercurrent desorption tower is 0.5-1.

9. The method for concentrating acetylene through partial oxidation of hydrocarbons according to claim 8, characterized in that: The ratio of the gas flow rate from the top of the countercurrent desorption tower to the gas flow rate is 0.7 or 0.

8.

10. A production system for the partial oxidation of hydrocarbons to acetylene, characterized in that: Includes the concentration apparatus according to any one of claims 1-7.

Images