CN218188898U - Selective direct oxidation desulfurization coupling liquid phase desulfurization process unit - Google Patents
Selective direct oxidation desulfurization coupling liquid phase desulfurization process unit Download PDFInfo
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- CN218188898U CN218188898U CN202222442266.4U CN202222442266U CN218188898U CN 218188898 U CN218188898 U CN 218188898U CN 202222442266 U CN202222442266 U CN 202222442266U CN 218188898 U CN218188898 U CN 218188898U
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Abstract
The utility model discloses a selectivity direct oxidation desulfurization coupling liquid phase desulfurization process units, it includes the acidizing fluid knockout drum, constant temperature reactor, the steam pocket, the sulphur condenser, the sulphur knockout drum, the sulphur jar that seals, the sulphur separator is through tentatively purifying the gas cooler and connecting the absorption tower, the absorption tower passes through the pregnant solution pump and connects the oxidation tower, the oxidation tower passes through the sulphur stuff pump and connects the pressure filter, the oxidation tower is connected to the pressure filter, oxidation fan is connected to the oxidation tower, the oxidation tower passes through the lean solution pump and connects the absorption tower, the pressure filter is connected and is joined in marriage the dressing trough, join in marriage the dressing trough and pass through thick liquid delivery pump and connect intermittent type sulfur melting cauldron, the steam pocket is connected to the intermittent type sulfur melting cauldron, the liquid sulfur pond. The utility model discloses especially in the operating mode of well, high latent sulphur volume operating mode and requirement high purification degree, with the coupling of selectivity direct oxidation desulfurization and liquid phase catalytic oxidation desulfurization process, both guaranteed the desorption efficiency of hydrogen sulfide, guaranteed the quality of lower cost and product sulphur again.
Description
Technical Field
The utility model relates to a selective direct oxidation desulfurization coupling liquid phase desulfurization process units belongs to gas purification technical field.
Background
The hydrogen sulfide belongs to highly toxic and inflammable chemicals and is widely present in natural gas, methane, coal gas and other gases. With the increasing importance of the country on environmental protection, the emission standard of sulfur-containing gas is also more strict. Among numerous hydrogen sulfide removal technologies, the selective direct oxidation desulfurization process device has the advantages of large treatment capacity, high sulfur product purity, simple operation, low investment and maintenance cost and the like, but because the oxygen-sulfur ratio is difficult to accurately control and the reaction conversion rate is limited, only about 95% of hydrogen sulfide in source gas can be converted in a constant temperature reactor, the rest hydrogen sulfide needs to enter an adiabatic reactor again for deep oxidation, when the hydrogen sulfide is converted into elemental sulfur, a small amount of hydrogen sulfide can be directly oxidized into sulfur dioxide, so that the total sulfur content of tail gas cannot meet the purification requirement, and the sulfur conversion rate is low. Therefore, the selective direct oxidation desulfurization process device is improved, and the popularization and the application of the technology are facilitated.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the defects of the prior art and provide a selective direct oxidation desulfurization coupling liquid-phase desulfurization process device.
The utility model provides a technical scheme as follows: a selective direct oxidation desulfurization coupling liquid phase desulfurization process device comprises an acid liquor separation tank, wherein the acid liquor separation tank and an air distribution fan are both connected to a source gas preheater, the source gas preheater is connected with a constant temperature reactor, the constant temperature reactor is respectively connected with a steam drum and a sulfur condenser, the sulfur condenser is respectively connected with a sulfur separator and a sulfur seal tank, the sulfur separator is connected with a sulfur seal tank, and the sulfur seal tank is connected with a liquid sulfur pool.
The utility model has the advantages that:
the utility model overcomes there has been the problem that the sulphur conversion rate of selective direct oxidation process units sulphur is low, the total sulphur content of tail gas exceeds standard, the adiabatic reactor and the tail gas washing jar of traditional process units have been cancelled, the substitute is that the purification gas directly gets into liquid phase catalytic oxidation desulphurization unit through the cooling after going out the constant temperature reactor, utilize the advantage of the high sulphur conversion rate of liquid phase catalytic oxidation desulfurization technique, turn into surplus hydrogen sulfide into sulphur, so both guaranteed the desorption efficiency of hydrogen sulfide, the quality of product sulphur has been guaranteed again, have easy operation concurrently simultaneously, advantages such as stable process, be particularly useful for in the sulphur load, big and require the exhaust gas desulfurization project of high purification degree.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
The following detailed description of embodiments of the present invention is provided with reference to the accompanying drawings:
as shown in fig. 1, a selective direct oxidation desulfurization coupling liquid-phase desulfurization process device comprises an acid liquor separation tank 1, a constant temperature reactor 2, a steam drum 3, a sulfur condenser 4, a sulfur separation tank 5, a sulfur seal tank 6, an absorption tower 7, an oxidation tower 8, a filter press 9, a slurry preparation tank 10, an intermittent sulfur melting kettle 11, a liquid sulfur pool 12, an air distribution fan 13, an oxidation fan 14, a source gas preheater 15, a primary purified gas cooler 16, a rich liquid pump 17, a sulfur slurry pump 18, a lean liquid pump 19 and a slurry delivery pump 20.
The gas outlet pipeline at the top of the acid liquor separation tank 1 is communicated with the pipeline of the air distribution fan 13 and is connected to the inlet pipeline of the source gas preheater 15, the outlet pipeline of the source gas preheater 15 is connected with the inlet of the thermostatic reactor 2, the cooling water inlet and the steam outlet on the upper part of the thermostatic reactor 2 are respectively connected with the cooling water outlet and the steam inlet of the steam pocket 3, the primary purified gas outlet of the thermostatic reactor 2 is connected with the inlet of the sulfur condenser 4 through a pipeline, the gas phase outlet of the sulfur condenser 4 is connected with the inlet of the sulfur separator 5 through a pipeline, the liquid sulfur outlet of the sulfur condenser 4 is connected with the inlet of the sulfur seal tank 6 through a pipeline, the outlet of the sulfur separator 5 is connected with the inlet of the sulfur seal tank 6 through a pipeline, and the outlet of the sulfur seal tank 6 is connected with the liquid sulfur pool 12 through a pipeline. The outlet of the sulfur separator 5 is connected with the inlet of the primary purified gas cooler 16 through a pipeline, the outlet of the primary purified gas cooler 16 is connected with the inlet of the absorption tower 7 through a pipeline, the bottom outlet of the absorption tower 7 is connected with the inlet of the rich liquid pump 17 through a pipeline, the outlet of the rich liquid pump 17 is connected with the rich liquid inlet of the oxidation tower 8 through a pipeline, the bottom sulfur slurry outlet of the oxidation tower 8 is connected with the inlet of the sulfur slurry pump 18 through a pipeline, the outlet of the sulfur slurry pump 18 is connected with the inlet of the filter press 9 through a pipeline, the filtrate outlet of the filter press 9 is connected with the filtrate inlet of the oxidation tower 8 through a pipeline, the oxidizing air inlet of the oxidation tower 8 is connected with the outlet of the oxidizing fan 14 through a pipeline, the lean liquid outlet of the oxidation tower 8 is connected with the inlet of the lean liquid pump 19 through a pipeline, and the outlet of the lean liquid pump 19 is connected with the lean liquid inlet of the absorption tower 7 through a pipeline. The filter press 9 is connected through the pipeline and is joined in marriage dressing trough 10, and the export of joining in marriage dressing trough 10 passes through the entry of pipe connection slurry delivery pump 20, and the export of slurry delivery pump 20 passes through the sulphur thick liquid entry of pipe connection intermittent type sulfur melting cauldron 11, and the steam inlet of intermittent type sulfur melting cauldron 11 passes through the steam outlet of pipe connection steam pocket 3, and the bottom liquid sulfur export of intermittent type sulfur melting cauldron 11 passes through pipe connection liquid sulfur pond 12.
During operation, the source gas firstly enters the acid liquor separation tank 1, entrained liquid is separated out, then the liquid is mixed with air from the air distribution fan 13, the molar ratio of oxygen to sulfur is controlled to be 0.6-0.8, and the mixture enters the constant temperature reactor 2 after being heated to 100-150 ℃ by the source gas preheater 15. In the constant temperature reactor 2, hydrogen sulfide in source gas reacts with oxygen under the action of a catalyst, most of the hydrogen sulfide is converted into sulfur and water and releases a large amount of heat, boiler water enters a tube array in the constant temperature reactor 2 through a steam drum 3, redundant heat is taken out and is changed into steam, the temperature in the constant temperature reactor 2 is maintained within 150-280 ℃, and generated steam with 0.5MPa enters the steam drum 3; gas-phase substances in the constant temperature reactor 2 enter a sulfur condenser 4 through a primary purified gas outlet and a pipeline, sulfur in the gas phase is changed into liquid, enters a sulfur seal tank 6 through a liquid sulfur outlet and a pipeline of the sulfur condenser 4, then enters a liquid sulfur pool 12, primary purified gas enters a sulfur separation tank 5, entrained sulfur is further separated, and then enters an absorption tower 7 after the temperature is reduced to 45-52 ℃ through a primary purified gas cooler 16; after entering an absorption tower 7, the primary purified gas is in countercurrent contact with the desulfurization solution from an oxidation tower 8, wherein unreacted hydrogen sulfide is converted into sulfur, the purified gas is discharged from the top of the absorption tower 7, the rich solution containing sulfur particles is discharged from the bottom of the absorption tower 7 and is pumped into the oxidation tower 8 by a rich solution pump 17, the desulfurization solution is in contact regeneration with the oxidizing air from an oxidizing fan 14 in the oxidation tower 8 and is pumped back to the absorption tower 7 by a barren solution pump 19, the air is directly emptied, the sulfur in the oxidation tower 8 naturally settles to the conical bottom and is pumped into a filter press 9 by a sulfur pump 18, the filter press 9 separates the sulfur from the filtrate, the sulfur is sent to a slurry distribution tank 10, and the filtrate returns to the oxidation tower 8; when the sulfur in the slurry preparation tank 10 is accumulated to a certain degree, fresh water is added to prepare 5wt% -20 wt% sulfur slurry, the slurry is pumped into an intermittent sulfur melting kettle 11 through a slurry delivery pump 20, the pressure in the intermittent sulfur melting kettle 11 is ensured to be 0.2-0.6 MPa, the temperature in the intermittent sulfur melting kettle 11 is kept at 120-180 ℃ through 0.5MPa steam in a steam pocket 3, the sulfur is melted into liquid sulfur, the liquid sulfur is sent to a liquid sulfur pool 12, and the residual wastewater is sent to a subsequent treatment device.
It should be understood that parts of the specification not set forth in detail are well within the prior art. The above embodiments are only described for the preferred embodiments of the present invention, and other preferred embodiments are not described one by one, and the scope of the present invention is not limited, and those skilled in the art can make various modifications and improvements to the technical solution of the present invention without departing from the design spirit of the present invention, and all should fall within the protection scope defined by the claims of the present invention.
Claims (1)
1. A selective direct oxidation desulfurization coupling liquid phase desulfurization process device comprises an acid liquor separation tank (1), wherein the acid liquor separation tank (1) and an air distribution fan (13) are both connected to a source gas preheater (15), the source gas preheater (15) is connected with a constant temperature reactor (2), the constant temperature reactor (2) is respectively connected with a steam drum (3) and a sulfur condenser (4), the sulfur condenser (4) is respectively connected with a sulfur separator (5) and a sulfur seal tank (6), the sulfur separator (5) is connected with a sulfur seal tank (6), the sulfur seal tank (6) is connected with a liquid sulfur pool (12), and the device is characterized in that the sulfur separator (5) is connected with an inlet of an absorption tower (7) through a primary purified gas cooler (16), the bottom outlet of the absorption tower (7) is connected with the rich liquor inlet of the oxidation tower (8) through a rich liquor pump (17), the bottom sulfur slurry outlet of the oxidation tower (8) is connected with the inlet of a filter press (9) through a sulfur slurry pump (18), the filtrate outlet of the filter press (9) is connected with the filtrate inlet of the oxidation tower (8), the oxidizing air inlet of the oxidation tower (8) is connected with the outlet of an oxidizing fan (14), the barren liquor outlet of the oxidation tower (8) is connected with the barren liquor inlet of the absorption tower (7) through a barren liquor pump (19), the filter press (9) is connected with a slurry preparation tank (10), the outlet of the slurry preparation tank (10) is connected with an intermittent sulfur melting kettle (11) through a slurry delivery pump (20) ) The steam inlet of the intermittent sulfur melting kettle (11) is connected with the steam outlet of the steam drum (3), and the liquid sulfur outlet at the bottom of the intermittent sulfur melting kettle (11) is connected with the liquid sulfur pool (12).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222442266.4U CN218188898U (en) | 2022-09-15 | 2022-09-15 | Selective direct oxidation desulfurization coupling liquid phase desulfurization process unit |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222442266.4U CN218188898U (en) | 2022-09-15 | 2022-09-15 | Selective direct oxidation desulfurization coupling liquid phase desulfurization process unit |
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| CN202222442266.4U Active CN218188898U (en) | 2022-09-15 | 2022-09-15 | Selective direct oxidation desulfurization coupling liquid phase desulfurization process unit |
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