CN210528467U - Selective oxidation sulfur recovery device - Google Patents
Selective oxidation sulfur recovery device Download PDFInfo
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- CN210528467U CN210528467U CN201921296330.4U CN201921296330U CN210528467U CN 210528467 U CN210528467 U CN 210528467U CN 201921296330 U CN201921296330 U CN 201921296330U CN 210528467 U CN210528467 U CN 210528467U
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Abstract
The utility model belongs to the technical field of coal chemical industry, and relates to a selective oxidation sulfur recovery device, which comprises a mixed gas unit, a primary reactor, a waste heat boiler, a condensation sulfur collector, a secondary reactor and a cooling recovery unit; the mixed gas unit comprises a separation tank, a fan, a heating tank and a mixing tank which are connected in sequence; the cooling and recovering unit comprises a condenser and a sulfur trap which are connected in sequence; the outlet of the mixed gas unit is finally connected with the inlet of the cold sulfur agglutinator through the tube side of the primary reactor and the tube side of the waste heat boiler; the outlet of the cold sulfur agglutinating device is respectively connected with the inlet of the heating tank of the mixed gas unit and the inlet of the secondary reactor; and the outlet of the secondary reactor is sequentially connected with a condenser and a sulfur trap. The utility model discloses simple process equipment is few, and the investment is little, and running cost is low, the rate of recovery is high, can the recovery processing different concentration hydrogen sulfide gas body.
Description
Technical Field
The utility model belongs to the technical field of the coal chemical industry, a sulfur recovery unit is related to, in particular to select oxidation sulfur recovery unit.
Background
In the chemical industry, especially in the coal chemical production, hydrogen sulfide gas is generated, and because the hydrogen sulfide gas is extremely toxic, even dilute hydrogen sulfide has stimulation effect on respiratory tract and eyes and causes headache, when the concentration reaches 1mg/L or higher, the hydrogen sulfide gas is dangerous to life, and the hydrogen sulfide gas is purified and can be discharged after reaching the discharge standard. With the stricter requirements of environmental protection standards, the higher the requirements of hydrogen sulfide recovery processing technology are in order to make the sulfur emission reach higher emission standards.
At present, the oxidation method has the advantages of large treatment capacity and continuous production, and is widely applied to industry. The oxidation method is divided into dry oxidation and wet oxidation; the wet oxidation is absorption catalytic oxidation in a solution, the process is complex, the solution is introduced, the energy consumption is high, the environment is not protected, the sulfur impurities in the product are more, and the sulfur form is not good; the dry oxidation is usually carried out to oxidize hydrogen sulfide gas into elemental sulfur or sulfur oxide, and has the characteristics of large treatment capacity and continuous production, typical dry oxidation comprises a Claus method and a selective oxidation method, the Claus process has more complex flow, high equipment investment and high operation cost; the selective oxidation process is simple and is suitable for treating gases containing hydrogen sulfide with various concentrations.
Disclosure of Invention
Based on the problem that exists among the above-mentioned background art, the utility model provides a simple process equipment is few, and the investment is little, and the running cost is low, the rate of recovery is high, can the recovery processing different concentration's hydrogen sulfide gas's selective oxidation sulphur recovery unit.
In order to realize the purpose, the utility model discloses the technical scheme who takes does:
the selective oxidation sulfur recovery device is characterized by comprising a mixed gas unit, a primary reactor, a waste heat boiler, a condensation sulfur collector, a secondary reactor and a cooling recovery unit; the outlet of the mixed gas unit is finally connected with the inlet of the cold sulfur agglutinator through the tube side of the primary reactor and the tube side of the waste heat boiler; the outlet of the cold sulfur agglutinating device is respectively connected with the inlet of the mixed gas unit and the inlet of the secondary reactor; the outlet of the secondary reactor is connected with a cooling and recovering unit;
the mixed gas unit comprises a separation tank, a fan, a heating tank and a mixing tank which are connected in sequence; the outlet of the mixing tank is connected with the inlet of the tube side of the primary reactor; the inlet of the heating tank is connected with the outlet of the condensation sulfur collector;
the tube side of the first-stage reactor is filled with a catalyst;
the cooling and recovering unit comprises a condenser and a sulfur trap which are connected in sequence; the outlet of the secondary reactor is connected with the inlet of the condenser.
The selective oxidation sulfur recovery device also comprises a steam drum; the tube side outlet of the steam drum is connected with the shell side inlet of the first-stage reactor; the shell side outlet of the first-stage reactor is connected with the tube side inlet of the steam drum; and the shell pass outlet of the steam drum is connected with the shell pass inlet of the heating tank.
The selective oxidation sulfur recovery device also comprises a start-up heater and a heat exchanger which are arranged between the outlet of the condensation sulfur collector and the inlet of the secondary reactor; the outlet of the cold sulfur agglutinator is divided into three branches; the first branch is that the outlet of the condensation sulfur collector is connected with the inlet of the secondary reactor through the start-up heater; the second branch is a bypass; and the third branch is that the outlet of the secondary reactor is connected with the inlet of the condenser through the heat exchanger, and the outlet of the cold sulfur condenser is connected with the inlet of the condenser through the heat exchanger.
And a heater is arranged on an outlet pipeline of the sulfur trap.
An included angle is formed between the central axis of the waste heat boiler and the horizontal line; the included angle is 5-15 degrees.
The catalyst is a titanium-based catalyst.
The utility model has the advantages that:
1. the utility model provides a selective oxidation sulfur recovery device, which comprises a mixed gas unit, a first-stage reactor, a waste heat boiler, a condensation sulfur collector, a second-stage reactor and a cooling recovery unit; the outlet of the mixed gas unit is finally connected with the inlet of the cold sulfur agglutinator through the tube side of the primary reactor and the tube side of the waste heat boiler; the outlet of the cold sulfur agglutinating device is respectively connected with the inlet of the mixed gas unit and the inlet of the secondary reactor; the outlet of the secondary reactor is connected with a cooling and recovering unit. The utility model discloses an equipment is less, and the investment is little.
2. The titanium-based catalyst is filled in the tube pass of the primary reactor; the catalyst has good activity and high desulfurization efficiency.
3. The utility model discloses one-level reaction desulfurization gas produces condensation gas behind waste heat boiler and cold agglutinate sulphur ware, and the feed gas in condensation gas brings the reaction gas of system into and forms the mist and get into the first order reactor reaction as circulating gas with hydrogen sulfide and oxygen, and the non-reaction gas that the raw materials brought into advances the second order reaction back and discharges for the desulfurization efficiency of technology further obtains improving.
4. The utility model provides a selection oxidation sulphur recovery unit is suitable for the desulfurization of the 3 ~ 98% hydrogen sulfide gas body of concentration to be retrieved, and the range of application is wide, and the sulphur rate of recovery is high, and the running cost is low.
Drawings
FIG. 1 is a schematic view of a process for recovering sulfur by isothermal selective oxidation;
wherein:
r001 — first stage reactor; r002-secondary reactor; v001-a separation tank; v002-mixing tank; v003-steam pocket; e001-heating tank; e002-waste heat boiler; e003, a condenser; e004-sulfur trap; e005-condensation sulfur collector; e006-start-up heater; e007-heat exchanger; e008-a heater; c001-a fan; c002-circulating fan;
1-hydrogen sulfide gas; 2-oxygen gas; 3-mixed gas; 4-primary reaction of the desulfurized gas; 5-desulfurization gas of the waste boiler; 6-primary condensing the gas; 7-recycle gas; 8-secondary reaction of the mixed gas; 9-secondary reaction of the desulfurized gas; 10-secondary condensation of the gas; 11-desulfurization tail gas; 12-medium pressure steam; 13-boiler water; and 14, waste liquid.
Detailed Description
The present invention will now be described in detail with reference to the accompanying drawings and examples.
Referring to fig. 1, the utility model provides a selective oxidation sulfur recovery device, including gas mixture unit, first order reactor R001, exhaust-heat boiler E002, condensation sulfur collector E005, second order reactor R002 and cooling recovery unit. The outlet of the mixed gas unit is finally connected with the inlet of a cold sulfur condenser E005 through the tube side of a primary reactor R001 and the tube side of a waste heat boiler E002, the outlet of the cold sulfur condenser E005 is respectively connected with the inlet of the mixed gas unit and the inlet of a secondary reactor R002, and the outlet of the secondary reactor R002 is connected with a cooling recovery unit; the mixed gas unit comprises a separation tank V001, a fan C002, a heating tank E001 and a mixing tank V002 which are connected in sequence, the outlet of the mixing tank V002 is connected with the inlet of the tube side of the first-stage reactor R001, and the outlet of the condensation sulfur collector E005 is connected with the inlet of the heating tank E001 and the inlet of the second-stage reactor R002 respectively; an included angle is formed between the central axis of the waste heat boiler E002 and the horizontal line; the included angle is 5-15 degrees, so that liquid sulfur of the primary reaction desulfurization gas 4 cooled by the waste heat boiler E002 enters a condensation current collector E005 along with the waste heat boiler desulfurization gas 5, and the liquid sulfur cannot be remained or entrained on the inner wall of the waste heat boiler E002; the cooling recovery unit comprises a condenser E003 and a sulfur trap E004 which are sequentially connected, and the outlet of the secondary reactor R002 is sequentially connected with the condenser E003 and the sulfur trap E004. The first-stage reactor R001 is a shell-and-tube reactor, and the tube side of the first-stage reactor is filled with a catalyst which is a titanium-based catalyst. The secondary reactor R002 is an adiabatic condensation reactor.
The selective oxidation sulfur recovery device provided by the utility model also comprises a steam pocket V003; the tube side outlet of the steam drum V003 is connected with the shell side inlet of the first-stage reactor R001; the shell side outlet of the first-stage reactor R001 is connected with the tube side inlet of the steam drum V003; the shell side outlet of the steam drum V003 is connected with the shell side inlet of the heating tank E001.
The selective oxidation sulfur recovery device provided by the utility model also comprises a start-up heater E006 and a heat exchanger E007 which are arranged between the outlet of the condensation sulfur collector E005 and the inlet of the secondary reactor R002; the outlet of the cold sulfur agglutinator E005 is divided into three branches; the first branch is that the outlet of the condensation sulfur collector E005 is connected with the inlet of the secondary reactor R002 through the start-up heater E006; the second branch is a bypass; the third branch is that the outlet of the secondary reactor R002 is connected with the inlet of the condenser E003 through the heat exchanger E007, and the outlet of the cold sulfur agglutinating device E005 is connected with the inlet of the condenser E003. And a heater E008 is arranged on an outlet pipeline of the sulfur trap E004.
The utility model provides a recovery process of isothermal selective oxidation sulfur, which comprises the following steps:
1) separating 3% -98% of hydrogen sulfide gas 1 by a separation tank V001, feeding the hydrogen sulfide gas 1 into a heating tank E001 by a fan C001 for heating, feeding the hydrogen sulfide gas 1 heated to a certain temperature into a mixing tank V002, and mixing the hydrogen sulfide gas with oxygen 2 directly introduced into the mixing tank V002 to obtain mixed gas 3, wherein the volume ratio of the oxygen 2 to the hydrogen sulfide gas 1 in the mixed gas 3 is 0.3-0.9;
2) the mixed gas 3 enters a primary reactor R001 from a tube side inlet of the primary reactor R001, and the mixed gas 3 is subjected to isothermal selective oxidation reaction in the primary reactor R001 under the conditions of a titanium-based catalyst and a reaction temperature of 140-350 ℃ to obtain primary reaction desulfurization gas 4; when isothermal selective oxidation reaction is carried out in the sequential reactor R001, a tube side outlet of the steam drum V003 is connected with a shell side inlet of the first-stage reactor R001, and a shell side outlet of the first-stage reactor R001 is connected with a tube side inlet of the steam drum V003, so that the temperature in the first-stage reactor R001 is kept within the range of 140-350 ℃, and thus the mixed gas 3 is subjected to isothermal selective oxidation reaction; the shell pass outlet of the steam drum V003 is connected with the shell pass inlet of the heating tank E001, and the medium-pressure steam from the shell pass of the steam drum V003 can heat the gas in the heating tank E001 or supply the gas to other boilers as required;
3) cooling the primary reaction desulfurization gas 4 in a waste heat boiler E002 to obtain waste boiler desulfurization gas 5;
4) the waste boiler desulfurization gas 5 enters a cold coagulation sulfur collector E005 to be condensed to obtain liquid sulfur and primary condensed gas 6, and the liquid sulfur enters a sulfur pool from an outlet at the bottom of the condensation sulfur collector E005; the primary condensed gas 5 is divided into two paths after coming out from an outlet at the top of a condensation sulfur collector E005, one path containing reaction gas is used as circulating gas 7 and returns to a heating tank E001 through a circulating fan C002 to be mixed with hydrogen sulfide gas 1 and oxygen gas 2 and then enters a primary reactor to react R001 for circulating reaction, and during specific implementation, the circulating amount of the circulating gas is determined according to the sulfur concentration in raw material gas and the sulfur concentration in the circulating gas together so as to ensure the recovery efficiency of sulfur; the non-reaction gas carried into the system by the other path of feed gas is taken as a secondary reaction mixed gas 8 and enters a secondary reactor R002 for secondary reaction after passing through a start-up heater E006;
5) the secondary reaction desulfurization gas 9 from the secondary reactor R002 passes through a heat exchanger E007 and then enters a condenser E003 to be condensed, so that secondary condensation gas 10 and liquid sulfur are obtained; liquid sulfur enters a sulfur pool from an outlet at the bottom of the condenser E003;
6) the secondary condensed gas 10 coming out of the top of the condenser E003 enters a sulfur trap E004 to further recover sulfur, and the sulfur trapping temperature is controlled to be 130-170 ℃ to obtain desulfurized tail gas 11 and liquid sulfur; and heating the desulfurization tail gas 11 to E008, then feeding into a boiler or carrying out oxidation catalytic treatment until the desulfurization tail gas reaches the standard, and discharging the liquid sulfur into a sulfur pool from an outlet at the bottom of a sulfur trap E004.
Example 1
The utility model provides a first order reactor R001 is the shell and tube type reactor, and second order reactor R002 is the cold tube reactor against current, and waste heat boiler E002's the central axis is 10 with the contained angle between the water flat line.
Adopt the utility model provides a when selecting the sulphur recovery unit of oxidation to carry out sulphur recovery processing, the concentration of hydrogen sulfide gas 1 is 35%, the concentration of oxygen gas 2 is 99.6%, the volume ratio of oxygen and hydrogen sulfide gas is 0.3, in getting into first order reactor R001 after blending tank V002 mixes, the temperature in first order reactor R001 is 140 ℃, catch sulphur ware E004 temperature control at 130 ℃, behind first order reactor R001 and second order reactor R002, the rate of recovery of sulphur is 98.6%, the sulphur content in the desulfurization tail gas 11 is 400mg/L, return low temperature methyl alcohol after the pressurization of desulfurization tail gas 11 and wash retreatment; but the amount of the desulfurization tail gas is less, so that the required power consumption is less.
Example 2
Different from the embodiment 1, the included angle between the central axis of the waste heat boiler E002 and the horizontal line is 5 degrees, the concentration of hydrogen sulfide gas 1 is 50 percent, the concentration of oxygen gas 2 is 99.6 percent, the volume ratio of oxygen to hydrogen sulfide gas is 0.42, the mixture is mixed by a mixing tank V002 and then enters a first-stage reactor R001, the temperature in the first-stage reactor R001 is 205 ℃, the temperature of a sulfur trap E004 is controlled at 150 ℃, the recovery rate of sulfur is 98.4 percent after the mixture passes through the first-stage reactor R001 and a second-stage reactor R002, and the sulfur content in the desulfurization tail gas 11 is 300 mg/L; the desulfurized tail gas 11 is returned to the boiler for treatment.
Example 3
Different from the embodiment 1, an included angle between a central axis of a waste heat boiler E002 and a horizontal line is 15 degrees, the concentration of hydrogen sulfide gas 1 is 3 percent, the concentration of oxygen gas 2 is 99.6 percent, the volume ratio of oxygen to hydrogen sulfide gas is 0.9, the mixture is mixed by a mixing tank V002 and then enters a first-stage reactor R001, the temperature in the first-stage reactor R001 is 340 ℃, the temperature of a sulfur trap E004 is controlled at 170 ℃, after passing through the first-stage reactor R001 and a second-stage reactor R002, the recovery rate of sulfur is 99 percent, and the sulfur content in the desulfurization tail gas 11 is 120 mg/L; and the desulfurized tail gas 11 reaches the standard and is discharged.
Example 4
Different from the embodiment 3, the included angle between the central axis of the waste heat boiler E002 and the horizontal line is 8 degrees, the concentration of the hydrogen sulfide gas 1 is 98 percent, the concentration of the oxygen gas 2 is 99.6 percent, the volume ratio of the oxygen gas to the hydrogen sulfide gas is 0.62, the mixture is mixed by the mixing tank V002 and then enters the first-stage reactor R001, the temperature in the first-stage reactor R001 is 265 ℃, the temperature of the sulfur trap E004 is controlled at 140 ℃, the recovery rate of sulfur is 98 percent after the mixture passes through the first-stage reactor R001 and the second-stage reactor R002, and the sulfur content in the desulfurization tail gas 11 is 700 mg/L; pressurizing the desulfurized tail gas 11, and returning to low-temperature methanol washing for retreatment; but the amount of the desulfurization tail gas is less, so that the required power consumption is less.
Example 5
Different from the embodiment 1, the included angle between the central axis of the waste heat boiler E002 and the horizontal line is 5 degrees, the concentration of hydrogen sulfide gas 1 is 75 percent, the concentration of oxygen gas 2 is 99.6 percent, the volume ratio of oxygen to hydrogen sulfide gas is 0.75, the mixture is mixed by a mixing tank V002 and then enters a first-stage reactor R001, the temperature in the first-stage reactor R001 is 255 ℃, the temperature of a sulfur trap E004 is controlled at 160 ℃, after passing through the first-stage reactor R001 and a second-stage reactor R002, the recovery rate of sulfur is 98 percent, and the sulfur content in the desulfurization tail gas 11 is 500 mg/L; the desulfurized tail gas 11 is returned to the boiler for treatment.
Claims (6)
1. The isothermal selective oxidation sulfur recovery device is characterized by comprising a mixed gas unit, a primary reactor (R001), a waste heat boiler (E002), a condensation sulfur collector (E005), a secondary reactor (R002) and a cooling recovery unit; the outlet of the mixed gas unit is finally connected with the inlet of the cold sulfur agglutinator (E005) through the tube side of the primary reactor (R001) and the tube side of the waste heat boiler (E002); the outlet of the cold sulfur agglutinator (E005) is respectively connected with the inlet of the mixed gas unit and the inlet of the secondary reactor (R002); the outlet of the secondary reactor (R002) is connected with a cooling recovery unit;
the mixed gas unit comprises a separation tank (V001), a fan (C001), a heating tank (E001) and a mixing tank (V002) which are connected in sequence; the outlet of the mixing tank (V002) is connected with the tube side inlet of the first-stage reactor (R001); the inlet of the heating tank (E001) is connected with the outlet of the cold sulfur agglutinator (E005);
the tube side of the first-stage reactor (R001) is filled with a catalyst;
the cooling recovery unit comprises a condenser (E003) and a sulfur trap (E004) which are connected in sequence; the inlet of the condenser (E003) is connected to the outlet of the secondary reactor (R002).
2. The isothermal selective oxidation sulfur recovery device according to claim 1, further comprising a steam drum (V003); the tube side outlet of the steam drum (V003) is connected with the shell side inlet of the primary reactor; the tube side inlet of the steam drum (V003) is connected with the shell side outlet of the primary reactor (R001); and the shell side outlet of the steam drum (V003) is connected with the shell side inlet of the heating tank (E001).
3. The isothermal selective oxidation sulfur recovery device according to claim 1, further comprising a start-up heater (E006) and a heat exchanger (E007) disposed between the outlet of the cold coagulation sulfur reactor (E005) and the inlet of the secondary reactor (R002); the outlet of the cold sulfur agglutinator (E005) is divided into three branches; the first branch is that the outlet of the cold condensed sulfur device (E005) is connected with the inlet of the secondary reactor (R002) through the start-up heater (E006); the second branch is a bypass; the third branch is that the outlet of the secondary reactor (R002) is connected with the inlet of the condenser (E003) through the heat exchanger (E007), and the outlet of the cold coagulation sulfur device (E005) is connected with the inlet of the condenser (E003) through the heat exchanger (E007).
4. The isothermal selective oxidation sulfur recovery device according to claim 3, wherein a heater (E008) is provided on the outlet pipeline of the sulfur trap (E004).
5. The isothermal selective oxidation sulfur recovery device according to claim 1 or 2 or 3 or 4, characterized in that the central axis of the waste heat boiler (E002) is at an angle to the horizontal; the included angle is 5-15 degrees.
6. The isothermal selective oxidation sulfur recovery device of claim 5, wherein the catalyst is a titanium-based catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921296330.4U CN210528467U (en) | 2019-08-09 | 2019-08-09 | Selective oxidation sulfur recovery device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921296330.4U CN210528467U (en) | 2019-08-09 | 2019-08-09 | Selective oxidation sulfur recovery device |
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| CN210528467U true CN210528467U (en) | 2020-05-15 |
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| CN201921296330.4U Active CN210528467U (en) | 2019-08-09 | 2019-08-09 | Selective oxidation sulfur recovery device |
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- 2019-08-09 CN CN201921296330.4U patent/CN210528467U/en active Active
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