CN210973883U - Sulfur recovery device is blown in circulation - Google Patents
Sulfur recovery device is blown in circulation Download PDFInfo
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- CN210973883U CN210973883U CN201921247884.5U CN201921247884U CN210973883U CN 210973883 U CN210973883 U CN 210973883U CN 201921247884 U CN201921247884 U CN 201921247884U CN 210973883 U CN210973883 U CN 210973883U
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Abstract
The utility model belongs to the technical field of the sulphur is retrieved, concretely relates to circulation blows sulphur recovery unit. The device comprises a reaction furnace, a waste heat boiler, a primary condenser, a primary heater, a primary reactor, a secondary condenser, a secondary heater, a secondary reactor, a tertiary condenser, a tail gas liquid separating tank, a tail gas heater, a hydrogenation reactor, a steam generator, a quench tower and an absorption tower which are connected in sequenceThe absorption tower comprises a tower, an incinerator and a chimney, a purified gas outlet of the absorption tower is also provided with a circulating gas pipeline which is respectively connected with inlets of the reaction furnace and the primary heater, and a circulating fan, a circulating air inlet and a circulating nitrogen inlet are arranged on the circulating gas pipeline. The device can reduce the emission of sulfur dioxide in flue gas to 100mg/Nm during the shutdown period of the sulfur recovery device3And the environment-friendly emission requirement is met, and the smoke is emitted up to the standard during the shutdown of the device. The circulating fan is used as power, so that the sealing operation is realized, and the nitrogen consumption is reduced.
Description
Technical Field
The utility model belongs to the technical field of the sulphur is retrieved, a sulphur recovery of oil refining, coal chemical industry, natural gas purification trade is related to, concretely relates to circulation blows sulphur recovery unit.
Background
The emission standard GB31570-2015 of the industrial pollutants for refining petroleum specifies that the emission concentration limit value of the atmospheric pollutants of the sulfur recovery device is less than 400mg/Nm3Especially less than 100mg/Nm3. The regulation does not set the flue gas SO during the startup and shutdown of the sulfur recovery device2The emission concentration is regulated, so the requirement of 'emission standard GB31570-2015 for petroleum refining industry pollutants' is met during start-up and shut-down periods, and the sulfur recovery device is more suitable for the start-up and shut-down periodsAnd (5) performing a great test.
Chinese patent CN106554000B discloses a green shutdown method of a sulfur recovery device, which comprises the steps of firstly cutting off acid gas entering a reaction furnace, then adopting absorption tower top purified gas, regeneration tower top acid gas, flue gas or any combination gas of the two and combustion dry gas or gas to sweep the reaction furnace, leading sweep tail gas to enter a first-stage reactor after passing through a first-stage sulfur condenser and a heat exchanger, leading sweep tail gas from the first-stage reactor to enter a second-stage reactor after passing through a second-stage sulfur condenser and the heat exchanger, leading sweep gas from the second-stage reactor to enter a third-stage sulfur condenser for condensation, mixing with hydrogen, leading the sweep gas to enter a hydrogenation reactor for hydrogenation to generate H2S, entering an absorption tower and a regeneration tower; the purified gas from the absorption tower is burnt in an incinerator and then discharged, and the acid gas regenerated from the regeneration tower can be used as blowing tail gas or directly enter other sulfur recovery devices for treatment. The method needs to pressurize the purified gas at the top of the absorption tower, the acid gas at the top of the regeneration tower and the flue gas and then introduce the pressurized gas into the reaction furnace for purging, and certain potential safety hazards exist in pressurization operation.
Chinese patent CN206521281U discloses a novel sulfur recovery device, wherein a reaction furnace, a waste heat boiler and a primary sulfur condenser are sequentially connected, a secondary sulfur condenser is arranged at the outlet of a primary reactor, a tertiary sulfur condenser is arranged at the outlet of a secondary reactor, liquid sulfur outlets of the primary, secondary and tertiary sulfur condensers are connected with a liquid sulfur pool, and a gas outlet of the tertiary sulfur condenser is connected with a tail gas treatment device; the inlet of the reaction furnace is connected with a purified air pipeline, a nitrogen pipeline and a sulfur production fan, the air outlet of the reaction furnace is connected with the inlet of the primary reactor, and the outlet of the waste heat boiler, the inlets of the primary reactor and the secondary reactor are respectively provided with a hot nitrogen conveying pipeline. The device has large nitrogen consumption and high energy consumption.
SUMMERY OF THE UTILITY MODEL
The utility model aims at developing a circulating sulfur-blowing sulfur recovery device, adopting the sulfur recovery device, the sulfur dioxide emission in the flue gas during the shutdown period of the sulfur recovery device can be less than 100mg/Nm3And the requirement of environmental protection emission is met, and the smoke emission reaching the standard during the shutdown of the device is realized. The device utilizes the circulating fan as power to realize the sealingThe closing operation reduces the nitrogen consumption; the controllability is high, and no side reaction occurs in the shutdown purging process; the total amount of tail gas is reduced, the load of the absorption tower is reduced, and the standard emission of flue gas during shutdown is ensured.
In order to achieve the purpose, the utility model is realized by adopting the following technical scheme:
the utility model provides a sulphur recovery unit is blown in circulation, including the reacting furnace that connects gradually, exhaust-heat boiler, the one-level condenser, the one-level heater, the one-level reactor, the second grade condenser, the second grade heater, the second grade reactor, tertiary condenser, tail gas divides the fluid reservoir, tail gas heater, hydrogenation ware, steam generator, the quench tower, the absorption tower, burn burning furnace and chimney, the liquid phase export of absorption tower is through the entry linkage of pipeline with the regenerator, the liquid phase export of regenerator is through the absorbent entry linkage of processing apparatus with the absorption tower, and connect the pipeline of above-mentioned each system and set up delivery pump, valve and be used for the instrument device of automatic control on the connecting tube, the tail gas export of tail gas divides the fluid reservoir to be provided with the entry linkage of pipeline and quench tower, the tail gas export of tower still is provided with the quench pipeline and burns the entry linkage of burning furnace, the gas export of absorption tower still is provided with the circulation gas pipeline, The inlet of the primary heater is connected, and a circulating fan, a circulating air inlet and a circulating nitrogen inlet are arranged on the circulating gas pipeline.
Further, a liquid phase outlet of the regeneration tower (23) is connected with an inlet of the amine liquid storage tank (22) through a pipeline, a gas phase at the top of the regeneration tower (23) is connected with the gas-liquid separation tank (30), a liquid phase outlet at the bottom of the gas-liquid separation tank (30) is connected with an inlet of the amine liquid storage tank (22), and a gas phase outlet of the gas-liquid separation tank (30) is connected with the aftertreatment system through a regenerated acid gas outlet (27); the outlet of the amine liquid storage tank (22) is connected with the absorbent inlet of the absorption tower (19).
Further, the rear part of the tail gas liquid separation tank is provided with an H2S/SO2And (4) a ratio meter.
Further, a hydrogen on-line analyzer is arranged at the gas outlet of the quenching tower.
Further, liquid sulfur outlets of the first-stage condenser, the second-stage condenser and the third-stage condenser are connected to a liquid sulfur pool.
Further, the primary heater, the secondary heater and the tail gas heater are medium-pressure steam heaters, on-line furnaces or gas-gas heat exchangers.
Adopt above-mentioned technical scheme, the beneficial effects of the utility model are that:
(1) the device can reduce the emission of sulfur dioxide in flue gas to 100mg/Nm during the shutdown period of the sulfur recovery device3And the environment-friendly emission requirement is met, and the smoke is emitted up to the standard during the shutdown of the device.
(2) The circulating fan is used as power, so that the sealing operation is realized, and the nitrogen consumption is reduced.
(3) No side reaction occurs in the shutdown purging process, and the temperature rise controllability of the catalyst bed layer is high.
(4) Reduce absorption tower load, ensure that the flue gas emission of reaching standard during the shutdown.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention, and together with the description serve to explain the invention and not to limit the invention.
In the drawings:
FIG. 1 is a flow chart of the recycling device for sulfur and sulfur by blowing of the present invention;
the respective symbols in the figure are as follows: 1 air inlet, 2 acid gas inlet, 3 reaction furnace, 4 exhaust-heat boiler, 5 first-stage condenser, 6 first-stage heater, 7 first-stage reactor, 8 second-stage condenser, 9 second-stage heater, 10 second-stage reactor, 11 third-stage condenser, 12 tail gas liquid separation tank, 13 tail gas heater, 14 hydrogenation reactor, 15 steam generator, 16 quench tower, 17 circulating water pump, 18 sewage outlet, 19 absorption tower, 20 rich solvent pump, 21 circulating fan, 22 amine liquid storage tank, 23 regeneration tower, 24 incinerator, 25 chimney, 26 liquid sulfur pool, 27 regenerated acid gas outlet, 28 circulating air inlet, 29 circulating nitrogen inlet, 30 gas-liquid separation tank, 31H gas inlet, 31H gas outlet, and the like2S/SO2A ratio meter and a 32 hydrogen on-line analyzer.
Detailed Description
In the description of the present invention, it should be noted that the terms "vertical", "upper", "lower", "horizontal", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention.
The present invention will be further explained with reference to the accompanying drawings.
As shown in figure 1, the utility model provides a sulphur recovery unit is blown in circulation, including reacting furnace 3, exhaust-heat boiler 4, one-level condenser 5, one-level heater 6, one-level reactor 7, second grade condenser 8, second grade heater 9, second grade reactor 10, tertiary condenser 11, tail gas divide liquid jar 12, tail gas heater 13, hydrogenation ware 14, steam generator 15, quench tower 16, absorption tower 19, burn burning furnace 24 and chimney 25 that connect gradually.
The air inlet 1 and the acid gas inlet 2 are connected with the reaction furnace, and the primary heater, the secondary heater and the tail gas heater are medium-pressure steam heaters.
The liquid sulfur outlets of the first-stage condenser, the second-stage condenser and the third-stage condenser are connected to a liquid sulfur pool 26.
The liquid phase outlet at the bottom of the quenching tower is connected with a circulating water pump 17, the quenching liquid discharged by the circulating water pump is discharged into a sewage treatment device through a sewage outlet 18, and part of the quenching liquid enters the quenching tower to cool the tail gas through cooling circulation.
The liquid phase outlet of the absorption column is connected to the inlet of the regeneration column 23 via a line on which a solvent pump 20 is provided. The liquid phase outlet of the regeneration tower is connected with the inlet of an amine liquid storage tank 22 through a pipeline, the gas phase at the top of the regeneration tower is connected with a gas-liquid separation tank 30, the bottom of the gas-liquid separation tank is connected with the amine liquid storage tank, the gas phase of the gas-liquid separation tank is treated by other devices through a regenerated acid gas outlet 27, and the liquid phase is connected with the inlet of the amine liquid storage tank. The outlet of the amine liquid storage tank is connected with the absorbent inlet of the absorption tower.
The tail gas outlet of the tail gas liquid separating tank is provided with a pipeline connected with the inlet of the quenching tower, the tail gas outlet of the quenching tower is also provided with a pipeline connected with the inlet of the incinerator, the purified gas outlet of the absorption tower is also provided with a circulating gas pipeline connected with the inlets of the reaction furnace and the primary heater respectively, and the circulating gas pipeline is provided with a circulating fan 21, a circulating air inlet 28 and a circulating nitrogen inlet 29.
The rear part of the tail gas separating tank is provided with H2S/SO2 A ratio meter 31 for detecting SO in the gas entering the inlet of the hydrogenation reactor in the circulating purging stage2The content of (a).
And a hydrogen on-line analyzer 32 is arranged at the gas outlet of the quenching tower, and the content of hydrogen in the gas at the outlet of the hydrogenation reactor is monitored in the circulating purging stage. H2Insoluble in water, and can react with hydrogen content at the outlet of the hydrogenation reactor when installed at the top of the quenching tower, such as at the outlet of the hydrogenation reactor or before and after a steam generator, and the long-term operation can cause H to be accumulated by sulfur2The analyzer jams, causing data distortion.
During use, the shutdown is divided into two stages, purging and passivating.
The blowing stage is to cut off the acid gas and air feed, and the tail gas heater, the hydrogenation reactor, the steam generator, the quench tower, the absorption tower and the regeneration tower are all operated normally. Establishing nitrogen circulation, injecting nitrogen from a circulating nitrogen inlet, blowing the nitrogen to the inlet of the reaction furnace and the inlet of the primary heater by a circulating fan, sequentially entering a primary reactor, a secondary condenser, a secondary heater, a secondary reactor, a tertiary condenser, a tail gas liquid separation tank, a tail gas heater, a hydrogenation reactor, a steam generator, a quench tower and an absorption tower along pipelines, and completing the circulation by the circulating fan.
Introducing the sweeping tail gas into a circulating nitrogen gas flow through a circulating nitrogen gas inlet, treating the sweeping tail gas by a hydrogenation reactor, hydrogenating sulfur-containing compounds which are not hydrogen sulfide in the hydrogenation reactor to generate hydrogen sulfide, quenching the hydrogen sulfide by a quenching tower, absorbing the hydrogen sulfide by an absorption tower, incinerating and discharging the hydrogen sulfide by an incinerator, and introducing the acid gas regenerated by a regeneration tower into other sulfur recovery devices which normally operate through pipelines for treatment. The inlet of the primary reactor is controlled to be 210-260 ℃, the inlet of the secondary reactor is controlled to be 220-240 ℃ and the inlet of the hydrogenation reactor is controlled to be 250-320 ℃ during the circulating sulfur blowing period.
And (3) performing a target practice test on the three-stage condenser at the later stage of purging, ending purging when no sulfur exists, and controlling the volume concentration of hydrogen in the gas at the outlet of the hydrogenation reactor to be not less than 1.0% by using a hydrogen online instrument during the period, and paying attention to the temperature rise of the bed layer of the hydrogenation reactor and the change of the pH value of the quenching water.
And (3) entering a passivation stage after the purging is finished, slowly injecting air into the nitrogen circulation from a circulating air inlet during the passivation, strictly controlling the oxygen content, gradually increasing the oxygen content from 0-10% according to the stage of 0.5%, passivating the pipeline and the catalyst, and if the bed layer has no obvious temperature rise, indicating that the passivation is finished.
Before passivation, amine liquid in the absorption tower is introduced into an amine liquid storage tank, and after the amine liquid is introduced into the amine liquid storage tank, the absorption tower and the regeneration tower are cut off from air flow through a pipeline between the top of the quench tower and the incinerator, and the absorption tower and the regeneration tower are in an empty tower state.
It is to be understood that the present invention has been described in detail with reference to the foregoing embodiments, and that modifications and equivalents of the various embodiments described above may be made by those skilled in the art, or some of the technical features may be substituted. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. A sulfur recovery device by circulating blowing comprises a reaction furnace (3), a waste heat boiler (4), a first-stage condenser (5), a first-stage heater (6), a first-stage reactor (7), a second-stage condenser (8), a second-stage heater (9), a second-stage reactor (10), a third-stage condenser (11), a tail gas separating tank (12), a tail gas heater (13), a hydrogenation reactor (14), a steam generator (15), a quench tower (16), an absorption tower (19), an incinerator (24) and a chimney (25) which are connected in sequence, wherein a liquid phase outlet of the absorption tower (19) is connected with an inlet of a regeneration tower (23) through a pipeline, a liquid phase outlet of the regeneration tower (23) is connected with an absorbent inlet of the absorption tower (19) through a treatment device, pipelines for connecting the systems, and a conveying pump, a valve and an instrument device for automatic control arranged on the connecting pipelines, the method is characterized in that:
the tail gas outlet of the tail gas liquid separation tank (12) is provided with a pipeline connected with an inlet of a quenching tower (16), the tail gas outlet of the quenching tower (16) is also provided with a pipeline connected with an inlet of an incinerator (24), a purified gas outlet of the absorption tower (19) is also provided with a circulating gas pipeline connected with inlets of a reaction furnace (3) and a primary heater (6) respectively, and a circulating fan (21), a circulating air inlet (28) and a circulating nitrogen inlet (29) are arranged on the circulating gas pipeline.
2. The recycling sulfur-blowing sulfur recovery device according to claim 1, wherein the liquid phase outlet of the regeneration tower (23) is connected with the inlet of the amine liquid storage tank (22) through a pipeline, the gas phase at the top of the regeneration tower (23) is connected with the gas-liquid separation tank (30), the liquid phase outlet at the bottom of the gas-liquid separation tank (30) is connected with the inlet of the amine liquid storage tank (22), and the gas phase outlet of the gas-liquid separation tank (30) is connected with the post-treatment system through the regenerated acid gas outlet (27); the outlet of the amine liquid storage tank (22) is connected with the absorbent inlet of the absorption tower (19).
3. The recycling sulfur-blowing sulfur recovery device according to claim 1, wherein the tail gas liquid separation tank (12) is provided with H at the rear part2S/SO2A ratio meter (31).
4. The recycling sulfur-blowing sulfur recovery device according to claim 1, characterized in that the outlet of the quenching tower (16) is provided with a hydrogen on-line analyzer (32).
5. The recycling sulfur blowing recovery device according to claim 1, wherein the liquid sulfur outlets of the primary condenser (5), the secondary condenser (8) and the tertiary condenser (11) are connected to a liquid sulfur pool (26).
6. The recycling sulfur-blowing sulfur recovery device according to claim 1, wherein the primary heater (6), the secondary heater (9) and the tail gas heater (13) are medium-pressure steam heaters, on-line furnaces or gas-gas heat exchangers.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921247884.5U CN210973883U (en) | 2019-08-02 | 2019-08-02 | Sulfur recovery device is blown in circulation |
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| CN201921247884.5U CN210973883U (en) | 2019-08-02 | 2019-08-02 | Sulfur recovery device is blown in circulation |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114275741A (en) * | 2021-12-31 | 2022-04-05 | 镇海石化工程股份有限公司 | Zero-emission shutdown method for flue gas pollutants of sulfur recovery device |
| CN114515509A (en) * | 2020-11-19 | 2022-05-20 | 中国石油天然气股份有限公司 | Shutdown desulfurization device and desulfurization method for sulfur recovery system |
| CN115340072A (en) * | 2022-09-14 | 2022-11-15 | 江西洪安化工有限公司 | Preparation system and method of sulfur dioxide gas |
-
2019
- 2019-08-02 CN CN201921247884.5U patent/CN210973883U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114515509A (en) * | 2020-11-19 | 2022-05-20 | 中国石油天然气股份有限公司 | Shutdown desulfurization device and desulfurization method for sulfur recovery system |
| CN114515509B (en) * | 2020-11-19 | 2023-10-31 | 中国石油天然气股份有限公司 | Shutdown sulfur removal device and method for sulfur recovery system |
| CN114275741A (en) * | 2021-12-31 | 2022-04-05 | 镇海石化工程股份有限公司 | Zero-emission shutdown method for flue gas pollutants of sulfur recovery device |
| CN114275741B (en) * | 2021-12-31 | 2023-12-19 | 镇海石化工程股份有限公司 | Zero-emission shutdown method for flue gas pollutants of sulfur recovery device |
| CN115340072A (en) * | 2022-09-14 | 2022-11-15 | 江西洪安化工有限公司 | Preparation system and method of sulfur dioxide gas |
| CN115340072B (en) * | 2022-09-14 | 2024-01-26 | 江西洪安化工有限公司 | Sulfur dioxide gas preparation system and method |
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