CN218188879U - Device for removing hydrogen sulfide in acid waste gas by direct oxidation method - Google Patents
Device for removing hydrogen sulfide in acid waste gas by direct oxidation method Download PDFInfo
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- CN218188879U CN218188879U CN202222442120.XU CN202222442120U CN218188879U CN 218188879 U CN218188879 U CN 218188879U CN 202222442120 U CN202222442120 U CN 202222442120U CN 218188879 U CN218188879 U CN 218188879U
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- 238000000034 method Methods 0.000 title claims abstract description 49
- 239000002253 acid Substances 0.000 title claims abstract description 34
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 229910000037 hydrogen sulfide Inorganic materials 0.000 title claims abstract description 26
- 239000002912 waste gas Substances 0.000 title claims abstract description 14
- 230000003647 oxidation Effects 0.000 title claims abstract description 13
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 13
- 239000007789 gas Substances 0.000 claims abstract description 98
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 80
- 239000007788 liquid Substances 0.000 claims abstract description 29
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 239000003054 catalyst Substances 0.000 claims abstract description 17
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000010936 titanium Substances 0.000 claims abstract description 8
- 229910052719 titanium Inorganic materials 0.000 claims abstract description 8
- 229910052717 sulfur Inorganic materials 0.000 claims description 69
- 239000011593 sulfur Substances 0.000 claims description 69
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- 230000002378 acidificating effect Effects 0.000 claims description 9
- 238000007789 sealing Methods 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- 238000009413 insulation Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000003795 desorption Methods 0.000 abstract description 2
- 239000005864 Sulphur Substances 0.000 abstract 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000006477 desulfuration reaction Methods 0.000 description 4
- 230000023556 desulfurization Effects 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model discloses a device of hydrogen sulfide in direct oxidation desorption acid waste gas, its sour liquid separator, air-blower link to each other with the acid gas preheater, and isothermal reactor, steam storage tank are connected to the acid gas preheater, and isothermal reactor connects steam storage tank, heat exchanger, and adiabatic reactor, sulphur condenser are connected to the heat exchanger, and adiabatic reactor, sulphur separator, sulphur seal jar are connected to the sulphur condenser, and the sulphur separator is connected and is washed alkaline jar, sulphur seal jar, and liquid sulphur pond is connected to sulphur seal jar. The utility model discloses can handle the acid waste gas of hydrogen sulfide concentration at 3 mol% ~35 mol% within range, use direct oxidation method, utilize titanium base catalyst, directly turn into the elemental sulfur with the hydrogen sulfide in the acid waste gas under 240 ℃. The utility model discloses equipment is small, area is little, and investment cost is low, and the gaseous hydrogen sulfide concentration of handling back is less than 5 ppm, retrieves sulphur quality one-level. The reaction heat is fully utilized in the hydrogen sulfide removal process, and the energy consumption is saved.
Description
Technical Field
The utility model relates to a device of hydrogen sulfide in direct oxidation desorption acid waste gas belongs to gas purification technical field.
Background
The complex iron wet desulphurization process is a mature hydrogen sulfide removal process, and has good hydrogen sulfide removal effect, so the complex iron wet desulphurization process is widely applied to the field of acid gas desulphurization. The existing complex iron wet desulphurization process device mostly adopts a double-tower process, namely, the absorption of hydrogen sulfide is realized in an absorption tower, the regeneration of a complex iron catalyst is realized in an oxidation tower, and in addition, a large amount of matched movable equipment is required to be equipped. Thus, this process installation has some drawbacks: 1. the requirement on the inlet pressure of the acid gas is high; 2. the air velocity of the absorption tower is usually only 40 to 120 m/h, and when the acid gas amount is larger or the concentration of hydrogen sulfide is higher, the volume of equipment is increased or the quantity of the equipment is increased, so that the occupied area is large, the investment is high, and the energy consumption is large; 3. the consumption of the desulfurizing agent is large, 4 percent, the total sulfur yield is low, the sulfur content in the tail gas is over-standard, 5 percent, and when the sulfur content is overlarge, the bottom of the equipment and the pipeline are easy to block. Therefore, it is necessary to develop a hydrogen sulfide removal device which can meet the requirement of deep desulfurization and has the advantages of low investment, low energy consumption and small occupied area.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the defects of the prior art and provide a device for removing hydrogen sulfide in acid waste gas by a direct oxidation method.
The utility model provides a technical scheme as follows: a device for removing hydrogen sulfide in acidic waste gas by a direct oxidation method comprises an acid-liquid separator, an acidic gas preheater connected with the acid-liquid separator, a heat exchanger and a liquid sulfur pool; the method is characterized in that a mixed gas inlet of the acid gas preheater is connected with a blower, and a mixed gas outlet of the acid gas preheater is connected with a mixed gas inlet of the isothermal reactor; a low-pressure steam inlet of the acid gas preheater is connected with a low-pressure steam outlet of the steam storage tank, and a condensed water outlet of the acid gas preheater is connected with a condensed water inlet of the isothermal reactor; a steam outlet of the isothermal reactor is connected with a steam inlet of a steam storage tank, the steam storage tank is provided with a boiler water inlet connected with an out-of-range boiler, a condensed water outlet of the steam storage tank is connected with a condensed water inlet of the isothermal reactor, and a process gas outlet of the isothermal reactor is connected with a first process gas inlet of the heat exchanger; a first process gas outlet of the heat exchanger is connected with a first process gas inlet of the sulfur condenser; the process gas outlet of the sulfur condenser is connected with the second process gas inlet of the heat exchanger; a second process gas outlet of the heat exchanger and the blower are connected with an inlet of the adiabatic reactor, and an outlet of the adiabatic reactor is connected with a second process gas inlet of the sulfur condenser; the tail gas outlet of the sulfur condenser is connected with the tail gas inlet of the sulfur separator, the tail gas outlet of the sulfur separator is connected with the inlet of the alkaline washing tank, the liquid sulfur outlet of the sulfur separator and the liquid sulfur outlet of the sulfur condenser are both connected with the inlet of the sulfur sealing tank, and the outlet of the sulfur sealing tank is connected with the inlet of the liquid sulfur pool.
Furthermore, the isothermal reactor comprises a reactor shell, wherein the upper end and the lower end of the reactor shell are respectively connected with an upper end enclosure and a lower end enclosure; the upper part in the reactor shell is a preheated heat insulation bed layer, the lower part is an isothermal reaction section provided with a coil heat exchanger, a titanium-based catalyst is filled in a coil gap of the coil heat exchanger, and the coil heat exchanger is connected with the reactor shell through a heat exchanger supporting beam; the upper end enclosure is provided with a mixed gas inlet, a condensed water outlet, a temperature measuring pipe orifice of the isothermal reaction section, a manhole of the upper end enclosure and a safety valve interface, the reactor shell is provided with a steam outlet, and the lower end enclosure is provided with a condensed water inlet and a process gas outlet.
Furthermore, the adiabatic reactor is cylindrical, a catalyst sieve plate is arranged below the adiabatic reactor, and a titanium-based catalyst is filled on the catalyst sieve plate.
The utility model has the advantages that:
(1) The air blower is used for distributing the acid waste gas and the process gas entering the adiabatic reactor, the proportion of oxygen and hydrogen sulfide is controlled to improve the reaction conversion rate, the sulfur content of tail gas is effectively reduced, and the problem of low source gas pressure is solved.
(2) The isothermal reactor with smaller volume is adopted to realize the removal of hydrogen sulfide in the acidic waste gas, the titanium-based catalyst in the isothermal reactor can be recycled, and the problems of large occupied area of an absorption tower and an oxidation tower, high investment and large consumption of desulfurization agents are solved.
(3) The adiabatic reactor is adopted, and the catalyst sieve plate is added in the adiabatic reactor to carry out deep desulfurization on the acidic waste gas, so that the problem that the sulfur content of the tail gas exceeds the standard is solved.
(4) A steam storage tank is arranged above the isothermal reactor to remove reaction heat in time and provide a heat source for the acid gas preheater, so that the operation energy consumption is reduced.
(5) The sulfur condenser is adopted to separate the liquid sulfur in the process gas in time, so that the reaction efficiency is improved, and the probability of equipment and pipeline blockage is reduced.
(6) The sulfur separator is adopted to separate and purify the liquid sulfur in the tail gas, so that the total sulfur yield of the device is improved.
(7) And the sulfur seal tank is adopted, so that the process gas in the sulfur recovery process is prevented from entering the liquid sulfur pool in a series manner, and the normal operation of the device is ensured.
(8) And (3) purifying the desulfurized tail gas by using an alkaline washing tank to ensure that the content of sulfur in the tail gas does not exceed the standard.
Drawings
Fig. 1 is a schematic structural view of the present invention;
fig. 2 is a schematic structural diagram of the isothermal reactor 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, the device for removing hydrogen sulfide in acidic waste gas by using a direct oxidation method comprises an acid-liquid separator 1, a blower 2, an acidic gas preheater 3, an isothermal reactor 4, a steam storage tank 5, a heat exchanger 6, an adiabatic reactor 7, a sulfur condenser 8, a sulfur separator 9, an alkaline washing tank 10, a sulfur seal tank 11 and a liquid sulfur pool 12. The adiabatic reactor 7 is cylindrical without a heat exchange component, a catalyst sieve plate 13 is arranged below the adiabatic reactor, and a titanium-based catalyst is filled on the catalyst sieve plate 13. A steam inlet and a low-pressure steam outlet are arranged above the steam storage tank 5, and a condensate water outlet and a boiler water inlet are arranged below the steam storage tank.
As shown in fig. 2, the isothermal reactor 4 includes a reactor shell 21, and the upper and lower ends of the reactor shell 21 are respectively connected to an upper end enclosure 17 and a lower end enclosure 23 through flanges. The upper part in the reactor shell 21 is a preheated adiabatic bed layer 19, the lower part is an isothermal reaction section provided with a coil heat exchanger 22, a titanium-based catalyst is filled in a coil gap of the coil heat exchanger 22, and the coil heat exchanger 22 is connected with the reactor shell 21 through a heat exchanger supporting beam 20. The upper end enclosure 17 is provided with a mixed gas inlet 14, a condensate outlet 16, an isothermal reaction section temperature measuring pipe orifice 15, an upper end enclosure manhole 27 and a safety valve interface 28, the isothermal reaction section temperature measuring pipe orifice 15 is used for installing a thermometer to monitor the temperature of the isothermal reaction section, the upper end enclosure manhole 27 is used for allowing relevant personnel to enter and exit so as to facilitate installation, maintenance and safety inspection, the safety valve interface 28 is used for connecting the safety valve, the reactor shell 21 is provided with a steam outlet 26, and the lower end enclosure 23 is provided with a condensate inlet 25 and a process gas outlet 24.
The outlet of the acid liquid separator 1 and the blower 2 are both connected with the mixed gas inlet of the acid gas preheater 3, and the mixed gas outlet of the acid gas preheater 3 is connected with the mixed gas inlet 14 of the isothermal reactor 4; a low-pressure steam inlet of the acid gas preheater 3 is connected with a low-pressure steam outlet of the steam storage tank 5, and a condensed water outlet of the acid gas preheater 3 is connected with a condensed water inlet 25 of the isothermal reactor 4; the steam outlet 26 of the isothermal reactor 4 is connected with the steam inlet of the steam storage tank 5, and the byproduct steam in the reaction process provides a heat source for the acid gas preheater 3. A boiler water inlet of the steam storage tank 5 is connected with an out-of-range boiler, a condensed water outlet of the steam storage tank 5 is connected with a condensed water inlet 25 of the isothermal reactor 4, and a process gas outlet 24 of the isothermal reactor 4 is connected with a first process gas inlet of the heat exchanger 6; a first process gas outlet of the heat exchanger 6 is connected with a first process gas inlet of the sulfur condenser 8; the process gas outlet of the sulfur condenser 8 is connected with the second process gas inlet of the heat exchanger 6; a second process gas outlet of the heat exchanger 6 and the blower 2 are both connected with an inlet of the adiabatic reactor 7, and an outlet of the adiabatic reactor 7 is connected with a second process gas inlet of the sulfur condenser 8; the tail gas outlet of the sulfur condenser 8 is connected with the tail gas inlet of the sulfur separator 9, the tail gas outlet of the sulfur separator 9 is connected with the inlet of the alkaline washing tank 10, the liquid sulfur outlet of the sulfur separator 9 and the liquid sulfur outlet of the sulfur condenser 8 are both connected with the inlet of the sulfur sealing tank 11, and the outlet of the sulfur sealing tank 11 is connected with the inlet of the liquid sulfur pool 12.
Separating the hydrogen sulfide-containing acidic waste gas into water, heavy hydrocarbon and the like in the gas through an acid-liquid separator 1, and then distributing the hydrogen sulfide-containing gas and oxygen entering from a blower 2 to form mixed gas; after being preheated to about 150 ℃ by the acid gas preheater 3, the mixed gas enters from the mixed gas inlet 14 of the isothermal reactor 4, is preheated to about 150 ℃ by the adiabatic bed 19, and then enters the isothermal reaction section, and the hydrogen sulfide in the mixed gas is converted into elemental sulfur. In the isothermal reactor 4, the reaction is a strong exothermic reaction, outside condensate water enters from a condensate water inlet 25 and flows out from a condensate water outlet 16 to cool the coil type heat exchanger 22, the temperature is maintained at about 240 ℃, and the flowing condensate water is recycled in a boiler; the heat released by a steam storage tank 5 arranged above the isothermal reactor 4 in the storage reaction process provides a heat source for the acid gas preheater 3. A large amount of heat released by the isothermal reaction section of the isothermal reactor 4 enters the steam storage tank 5 through a steam outlet 26 of the isothermal reactor 4 in the form of steam, boiler water from a boiler enters from a boiler water inlet of the steam storage tank 5 and is heated into low-pressure steam by a large amount of steam by-produced from the isothermal reaction section, and the low-pressure steam enters from a low-pressure steam inlet of the acid gas preheater 3 as a heat source of the acid gas preheater 3 to preheat mixed gas. And a condensed water outlet of the acid gas preheater 3 and a condensed water outlet of the steam storage tank 5 are connected with a condensed water inlet 25 of the isothermal reactor 4 to jointly cool the isothermal reaction section. The process gas at the outlet of the isothermal reactor 4 is subjected to heat exchange and cooling through a heat exchanger 6 and then enters a sulfur condenser 8 to separate liquid sulfur, the cooled process gas is heated through the heat exchanger 6 and is distributed again and then enters an adiabatic reactor 7, the residual hydrogen sulfide in the adiabatic reactor 7 is deeply oxidized into sulfur dioxide in a catalyst sieve plate 13 below the inside of the adiabatic reactor 7, the concentration of the hydrogen sulfide is ensured to be lower than 5 ppm, and the process gas subjected to deep desulfurization enters the sulfur condenser 8 again to separate the liquid sulfur; the purified gas passes through a sulfur separator 9 to separate liquid sulfur, is purified again through an alkaline washing tank 10, and is finally sent to an incinerator; the liquid sulfur in the sulfur condenser 8 enters a liquid sulfur pool 12 through a sulfur seal tank 11 for subsequent treatment.
It should be understood that parts of the specification not set forth in detail are of the prior art. The above embodiments are only described for the preferred embodiments of the present invention, and other preferred embodiments are not mentioned one by one, and the scope of the present invention is not limited, and the technical solution of the present invention can be modified and improved by those skilled in the art without departing from the spirit of the present invention.
Claims (3)
1. A device for removing hydrogen sulfide in acid waste gas by a direct oxidation method comprises an acid-liquid separator (1), an acid gas preheater (3) connected with the acid-liquid separator (1), a heat exchanger (6) and a liquid sulfur pool (12); the method is characterized in that a mixed gas inlet of the acid gas preheater (3) is connected with the blower (2), and a mixed gas outlet of the acid gas preheater (3) is connected with a mixed gas inlet of the isothermal reactor (4); a low-pressure steam inlet of the acid gas preheater (3) is connected with a low-pressure steam outlet of the steam storage tank (5), a steam outlet of the isothermal reactor (4) is connected with a steam inlet of the steam storage tank (5), a boiler water inlet connected with an out-of-range boiler is arranged on the steam storage tank (5), a condensate water outlet of the steam storage tank (5) is connected with a condensate water inlet of the isothermal reactor (4), and a process gas outlet of the isothermal reactor (4) is connected with a first process gas inlet of the heat exchanger (6); a first process gas outlet of the heat exchanger (6) is connected with a first process gas inlet of the sulfur condenser (8); a process gas outlet of the sulfur condenser (8) is connected with a second process gas inlet of the heat exchanger (6); a second process gas outlet of the heat exchanger (6) and the air blower (2) are connected with an inlet of the adiabatic reactor (7), and an outlet of the adiabatic reactor (7) is connected with a second process gas inlet of the sulfur condenser (8); the tail gas outlet of the sulfur condenser (8) is connected with the tail gas inlet of the sulfur separator (9), the tail gas outlet of the sulfur separator (9) is connected with the inlet of the alkaline washing tank (10), the liquid sulfur outlet of the sulfur separator (9) and the liquid sulfur outlet of the sulfur condenser (8) are both connected with the inlet of the sulfur sealing tank (11), and the outlet of the sulfur sealing tank (11) is connected with the inlet of the liquid sulfur pool (12).
2. The device for removing hydrogen sulfide in acidic exhaust gas by direct oxidation according to claim 1, wherein the isothermal reactor (4) comprises a reactor shell (21), and the upper end and the lower end of the reactor shell (21) are respectively connected with an upper end closure (17) and a lower end closure (23); the upper part in the reactor shell (21) is a preheated heat insulation bed layer (19), the lower part is an isothermal reaction section provided with a coil heat exchanger (22), a titanium-based catalyst is filled in a coil gap of the coil heat exchanger (22), and the coil heat exchanger (22) is connected with the reactor shell (21) through a heat exchanger supporting beam (20); a mixed gas inlet (14), a condensate outlet (16), an isothermal reaction section temperature measuring pipe orifice (15), an upper end cover manhole (27) and a safety valve interface (28) are arranged on the upper end cover (17), a steam outlet (26) is arranged on the reactor shell (21), and a condensate inlet (25) and a process gas outlet (24) are arranged on the lower end cover (23).
3. The apparatus for removing hydrogen sulfide from acidic exhaust gas by direct oxidation according to claim 1, wherein the adiabatic reactor (7) is cylindrical, a catalyst sieve plate (13) is arranged below the adiabatic reactor, and the catalyst sieve plate (13) is filled with a titanium-based catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222442120.XU CN218188879U (en) | 2022-09-15 | 2022-09-15 | Device for removing hydrogen sulfide in acid waste gas by direct oxidation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222442120.XU CN218188879U (en) | 2022-09-15 | 2022-09-15 | Device for removing hydrogen sulfide in acid waste gas by direct oxidation method |
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| Publication Number | Publication Date |
|---|---|
| CN218188879U true CN218188879U (en) | 2023-01-03 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202222442120.XU Active CN218188879U (en) | 2022-09-15 | 2022-09-15 | Device for removing hydrogen sulfide in acid waste gas by direct oxidation method |
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| Country | Link |
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| CN (1) | CN218188879U (en) |
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- 2022-09-15 CN CN202222442120.XU patent/CN218188879U/en active Active
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