CN115321489A - Sulfur recovery device and method - Google Patents
Sulfur recovery device and method Download PDFInfo
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- CN115321489A CN115321489A CN202110505682.1A CN202110505682A CN115321489A CN 115321489 A CN115321489 A CN 115321489A CN 202110505682 A CN202110505682 A CN 202110505682A CN 115321489 A CN115321489 A CN 115321489A
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- 238000000034 method Methods 0.000 title claims abstract description 148
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 142
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 47
- 239000011593 sulfur Substances 0.000 title claims abstract description 47
- 238000011084 recovery Methods 0.000 title claims abstract description 44
- 239000007789 gas Substances 0.000 claims abstract description 219
- 238000006243 chemical reaction Methods 0.000 claims abstract description 117
- 239000003054 catalyst Substances 0.000 claims abstract description 93
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 69
- 238000002485 combustion reaction Methods 0.000 claims abstract description 69
- 239000003546 flue gas Substances 0.000 claims abstract description 69
- 239000002737 fuel gas Substances 0.000 claims abstract description 48
- 239000002253 acid Substances 0.000 claims abstract description 27
- 239000003570 air Substances 0.000 claims abstract description 6
- 238000010438 heat treatment Methods 0.000 claims description 69
- 238000001816 cooling Methods 0.000 claims description 61
- 238000003303 reheating Methods 0.000 claims description 41
- 238000010517 secondary reaction Methods 0.000 claims description 34
- 239000002918 waste heat Substances 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 20
- 239000005864 Sulphur Substances 0.000 claims description 11
- 238000004891 communication Methods 0.000 claims description 7
- 230000001376 precipitating effect Effects 0.000 claims description 4
- 239000000567 combustion gas Substances 0.000 claims description 3
- 238000007872 degassing Methods 0.000 claims description 3
- 230000006641 stabilisation Effects 0.000 claims description 2
- 238000011105 stabilization Methods 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 10
- 239000003345 natural gas Substances 0.000 abstract description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 14
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 8
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000007670 refining Methods 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
- C01B17/0452—Process control; Start-up or cooling-down procedures of the Claus process
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
- C01B17/0426—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the catalytic conversion
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Automation & Control Theory (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The application provides a sulfur recovery device and a method, and belongs to the technical field of natural gas. The device comprises a combustion unit, a first bypass valve, a first-stage cold and hot unit, a first-stage reaction unit, a second bypass valve, a second-stage cold and hot unit, a second-stage reaction unit and a third-stage cold and hot unit; one side of the combustion unit is provided with a feed inlet for inputting fuel gas, air and acid gas; the discharge port of the combustion unit is also communicated with the feed inlet of the first-stage reaction unit through a first bypass valve, and the discharge port of the first-stage reaction unit is also communicated with the feed inlet of the second-stage reaction unit through a second bypass valve; and the combustion unit is used for combusting the fuel gas and the air to generate inert flue gas under the condition that the first bypass valve and the second bypass valve are opened, the inert flue gas sequentially passes through the first bypass valve, the first-stage reaction unit, the second bypass valve and the second-stage reaction unit, and the temperature of the first-stage catalyst bed layer in the first-stage reaction unit and the second-stage catalyst bed layer in the second-stage reaction unit is raised, so that the recovery efficiency of the elemental sulfur is improved.
Description
Technical Field
The application relates to the technical field of natural gas and petroleum, in particular to a sulfur recovery device and a method.
Background
In the natural gas purification and oil refining processes, a sulfur recovery device is usually required to recover and treat acid gas in the natural gas purification and oil refining processes so as to obtain a recovered product elemental sulfur. When the sulfur recovery device works, the temperature of a catalyst bed layer of the sulfur recovery device needs to be raised through high-temperature gas so as to meet the temperature condition of acid gas reaction; high-temperature gas is also needed to heat the catalyst bed layer during the non-working period of the sulfur recovery device so as to vaporize and remove the elemental sulfur on the catalyst bed layer. Therefore, how to raise the temperature of the catalyst bed layer is very important for recovering the elemental sulfur.
In the related technology, when the catalyst bed is heated by high-temperature gas, the route of the high-temperature gas is the same as the route of the acid gas for producing elemental sulfur in the sulfur recovery device, and the high-temperature gas reaches the catalyst bed after sequentially passing through the cooling assembly and the heating assembly. When high-temperature gas enters the catalyst bed layer through the route, the high-temperature gas needs to be cooled and then heated, so that time and labor are wasted, and the recovery efficiency of elemental sulfur is reduced.
Disclosure of Invention
The embodiment of the application provides a sulfur recovery device and a method, which can improve the recovery efficiency of elemental sulfur. The technical scheme is as follows:
on the one hand, the sulfur recovery device is provided, and the device comprises a combustion unit, a first bypass valve, a primary cold and hot unit, a primary reaction unit, a second bypass valve, a secondary cold and hot unit, a secondary reaction unit and a tertiary cold and hot unit;
the combustion unit, the primary cooling and heating unit, the primary reaction unit, the secondary cooling and heating unit, the secondary reaction unit and the tertiary cooling and heating unit are communicated in sequence;
a feed inlet is formed in one side of the combustion unit and used for inputting fuel gas, air and acid gas;
the discharge hole of the combustion unit is also communicated with the feed inlet of the first-stage reaction unit through the first bypass valve, and the discharge hole of the first-stage reaction unit is also communicated with the feed inlet of the second-stage reaction unit through the second bypass valve;
the combustion unit is used for combusting the fuel gas and the air to generate inert flue gas under the condition that the first bypass valve and the second bypass valve are opened, and the inert flue gas sequentially passes through the first bypass valve, the first-stage reaction unit, the second bypass valve and the second-stage reaction unit so as to heat a first-stage catalyst bed layer in the first-stage reaction unit and a second-stage catalyst bed layer in the second-stage reaction unit;
the combustion unit is further used for combusting the fuel gas and the air and reacting the acid gas and the air to generate a process gas under the condition that the first bypass valve and the second bypass valve are closed, and the process gas sequentially passes through the primary cold and hot unit, the primary reaction unit, the secondary cold and hot unit, the secondary reaction unit and the tertiary cold and hot unit;
the primary cooling and heating unit, the secondary cooling and heating unit and the tertiary cooling and heating unit are used for condensing the process gas, separating out elemental sulfur and heating the process gas for output;
the first-stage reaction unit and the second-stage unit are used for enabling the heated process gas to respectively carry out Claus reaction on the first-stage catalyst bed layer and the second-stage catalyst bed layer which are heated to generate elemental sulfur.
In one possible implementation, the combustion unit comprises a combustion furnace and a waste heat boiler;
a feed inlet is formed in one side of the combustion furnace and used for inputting the fuel gas, the air and the acid gas;
the discharge hole of the combustion furnace is communicated with the feed inlet of the waste heat boiler, and the discharge hole of the waste heat boiler is respectively communicated with the primary cold and hot unit and the primary reaction unit through the first bypass valve;
the combustion furnace is used for combusting the fuel gas and the air to generate inert flue gas under the condition that the first bypass valve and the second bypass valve are opened, and inputting the inert flue gas into the waste heat boiler;
the waste heat boiler is used for receiving the inert flue gas, enabling the inert flue gas to sequentially pass through the first bypass valve, the first-stage reaction unit, the second bypass valve and the second-stage reaction unit after the temperature of the inert flue gas is stabilized, and heating the first-stage catalyst bed layer and the second-stage catalyst bed layer;
the combustion furnace is also used for enabling the fuel gas to be combusted with the air and the acid gas to be reacted with the air under the condition that the first bypass valve and the second bypass valve are closed to generate a process gas, and the process gas is input into the waste heat boiler;
the waste heat boiler is used for receiving the process gas, and after the process gas is subjected to temperature stabilization, the process gas sequentially passes through the first-stage cold and hot unit, the first-stage reaction unit, the second-stage cold and hot unit, the second-stage reaction unit and the third-stage cold and hot unit.
In one possible implementation, the primary cold and hot unit comprises a primary condenser and a primary reheating furnace;
the feed port of the primary condenser is communicated with the discharge port of the combustion unit, the discharge port of the primary condenser is communicated with the first feed port of the primary reheating furnace, and the discharge port of the primary reheating furnace is communicated with the feed port of the primary reaction unit;
the primary condenser is used for condensing the process gas, separating out the elemental sulfur, and inputting the process gas separated out the elemental sulfur into the primary reheating furnace;
and the primary reheating furnace is used for receiving the process gas, heating the process gas and inputting the heated process gas into the primary reaction unit.
In a possible implementation manner, a second feed port is further formed in one side of the primary reheating furnace, and the second feed port is used for inputting combustion gas and air;
the primary reheating furnace is used for combusting the fuel gas and the air so as to heat the process gas.
In one possible implementation, the secondary cooling and heating unit comprises a secondary condenser and a secondary reheating furnace;
the feed port of the secondary condenser is communicated with the discharge port of the primary reaction unit, the discharge port of the secondary condenser is communicated with the first feed port of the secondary reheating furnace, and the discharge port of the secondary reheating furnace is communicated with the feed port of the secondary reaction unit;
the secondary condenser is used for condensing the process gas, separating out the elemental sulfur, and inputting the process gas separated out the elemental sulfur into the secondary reheating furnace;
and the secondary reheating furnace is used for receiving the process gas, heating the process gas and inputting the heated process gas into the secondary reaction unit.
In a possible implementation manner, a second feeding hole is further formed in one side of the secondary reheating furnace and used for inputting fuel gas and air;
the secondary reheating furnace is used for combusting the fuel gas and the air so as to heat the process gas.
In one possible implementation, the three-stage cold-hot unit comprises a three-stage condenser and an off-gas trap;
the feed inlet of the third-stage condenser is communicated with the discharge outlet of the second-stage reaction unit, and the discharge outlet of the third-stage condenser is communicated with the feed inlet of the tail gas catcher;
the three-stage condenser is used for condensing the process gas, separating out the elemental sulfur, and inputting the process gas separated out the elemental sulfur into the tail gas catcher;
the tail gas catcher is used for receiving the process gas, catching elemental sulfur in the process gas after heating the process gas, and outputting tail gas in the process gas.
In a possible implementation manner, the device further comprises a tail gas incinerator, wherein a feed inlet of the tail gas incinerator is communicated with a discharge outlet of the tail gas catcher;
and the tail gas incinerator is used for receiving the tail gas output by the tail gas catcher and incinerating the tail gas.
In a possible implementation manner, the device further comprises a liquid sulfur pool, and the liquid sulfur pool is respectively communicated with the discharge ports of the primary cold and hot unit, the secondary cold and hot unit and the tertiary cold and hot unit;
the liquid sulfur pool is used for receiving the elemental sulfur output by the first-stage cold and hot unit, the second-stage cold and hot unit and the third-stage cold and hot unit, and storing the elemental sulfur after degassing.
In another aspect, there is provided a process for the recovery of sulphur, the process comprising:
opening the first and second bypass valves;
controlling the combustion unit to enable the fuel gas and the air to be combusted to generate inert flue gas, wherein the inert flue gas sequentially passes through the first bypass valve, the first-stage reaction unit, the second bypass valve and the second-stage reaction unit to heat a first-stage catalyst bed layer in the first-stage reaction unit and a second-stage catalyst bed layer in the second-stage reaction unit;
closing the first and second bypass valves;
controlling the combustion unit to enable the fuel gas to be combusted with the air and the acid gas to be reacted with the air to generate process gas, and enabling the process gas to sequentially pass through the primary cold and hot unit, the primary reaction unit, the secondary cold and hot unit, the secondary reaction unit and the tertiary cold and hot unit;
controlling the primary cooling and heating unit, the secondary cooling and heating unit and the tertiary cooling and heating unit, condensing the process gas, separating out elemental sulfur, and heating and outputting the process gas;
controlling the first-stage reaction unit and the second-stage unit to enable the heated process gas to respectively perform Claus reaction in the first-stage catalyst bed layer and the second-stage catalyst bed layer which are heated to generate elemental sulfur;
opening the first bypass valve and the second bypass valve;
and controlling the combustion unit to enable the fuel gas and the air to be combusted to generate inert flue gas, wherein the inert flue gas sequentially passes through the first bypass valve, the first-stage reaction unit, the second bypass valve and the second-stage reaction unit to heat the first-stage catalyst bed layer and the second-stage catalyst bed layer, so that elemental sulfur on the first-stage catalyst bed layer and the second-stage catalyst bed layer is vaporized and removed.
The technical scheme provided by the embodiment of the application has the beneficial effects that at least:
the embodiment of the application provides a sulfur recovery device, the device is through setting up first bypass valve and second bypass valve, the inert flue gas that makes the combustion unit produce can pass one-level reaction unit and second grade reaction unit in proper order, heaies up to one-level catalyst bed and second grade catalyst bed respectively, has avoided raising the temperature again after the inert flue gas cooling, labour saving and time saving, and then has improved the efficiency that heaies up to one-level catalyst bed and second grade catalyst bed to the efficiency of elemental sulfur recovery has been improved.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings required to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the description below are only some embodiments of the present application, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
FIG. 1 is a schematic view of a sulfur recovery apparatus according to an embodiment of the present invention;
FIG. 2 is a block diagram of a sulfur recovery apparatus according to an embodiment of the present invention;
FIG. 3 is a flow chart of a sulfur recovery method according to an embodiment of the present application.
The reference numerals in the drawings denote:
10-a combustion unit;
101-a combustion furnace;
102-a waste heat boiler;
20-a first bypass valve;
30-a primary cold and hot unit;
301-first stage condenser;
302-primary reheating furnace;
40-first order reaction unit;
401-first order claus reactor;
50-a second bypass valve;
60-a secondary cooling and heating unit;
601-a secondary condenser;
602-secondary reheating furnace;
70-a secondary reaction unit;
701-a secondary claus reactor;
80-a three-stage cold and hot unit;
801-three-stage condenser;
802-an exhaust trap;
90-liquid sulfur pool;
100-gate valve.
Detailed Description
To make the objects, technical solutions and advantages of the present application more clear, the following detailed description of the embodiments of the present application will be made with reference to the accompanying drawings.
The terms "first," "second," "third," and "fourth," etc. in the description and claims of this application and in the accompanying drawings are used for distinguishing between different objects and not for describing a particular order. Furthermore, the terms "comprising" and "having," as well as any variations thereof, are intended to cover non-exclusive inclusions. For example, a process, method, system, article, or apparatus that comprises a list of steps or elements is not limited to only those steps or elements listed, but may alternatively include other steps or elements not listed, or inherent to such process, method, article, or apparatus.
The embodiment of the application provides a sulfur recovery device, referring to fig. 1, the device comprises a combustion unit 10, a first bypass valve 20, a primary cold and hot unit 30, a primary reaction unit 40, a second bypass valve 50, a secondary cold and hot unit 60, a secondary reaction unit 70 and a tertiary cold and hot unit 80. The combustion unit 10, the primary cooling and heating unit 30, the primary reaction unit 40, the secondary cooling and heating unit 60, the secondary reaction unit 70 and the tertiary cooling and heating unit 80 are sequentially communicated.
One side of the combustion unit 10 is provided with a feed inlet for inputting fuel gas, air and acid gas. The discharge port of the combustion unit 10 is also communicated with the feed port of the first-stage reaction unit 40 through the first bypass valve 20, and the discharge port of the first-stage reaction unit 40 is also communicated with the feed port of the second-stage reaction unit 70 through the second bypass valve 50.
And the combustion unit 10 is used for combusting the fuel gas and the air to generate inert flue gas under the condition that the first bypass valve 20 and the second bypass valve 50 are opened, wherein the inert flue gas sequentially passes through the first bypass valve 20, the primary reaction unit 40, the second bypass valve 50 and the secondary reaction unit 70 so as to heat a primary catalyst bed layer in the primary reaction unit 40 and a secondary catalyst bed layer in the secondary reaction unit 70.
The combustion unit 10 is further configured to combust the fuel gas with air and react the acid gas with air to generate a process gas, with the first bypass valve 20 and the second bypass valve 50 closed, and the process gas passes through the primary cooling and heating unit 30, the primary reaction unit 40, the secondary cooling and heating unit 60, the secondary reaction unit 70, and the tertiary cooling and heating unit 80 in sequence.
The first-stage cold and hot unit 30, the second-stage cold and hot unit 60 and the third-stage cold and hot unit 80 are used for condensing the process gas, separating out elemental sulfur, and heating the process gas for output.
The first-stage reaction unit 40 and the second-stage unit are used for enabling the heated process gas to respectively perform a Claus reaction on the first-stage catalyst bed layer and the second-stage catalyst bed layer which are heated to generate elemental sulfur.
The embodiment of the application provides a sulfur recovery device, the device is through setting up first bypass valve 20 and second bypass valve 50, the inertia flue gas that makes combustion unit 10 produce can pass one-level reaction unit 40 and second grade reaction unit 70 in proper order, heat up one-level catalyst bed and second grade catalyst bed respectively, avoided raising the temperature again after cooling the inertia flue gas, time saving and labor saving, and then improved the efficiency of raising the temperature to one-level catalyst bed and second grade catalyst bed, thereby the efficiency of elemental sulfur recovery has been improved.
Referring to fig. 2, the apparatus further comprises a liquid sulfur pool 90, and the liquid sulfur pool 90 is respectively communicated with the discharge ports of the primary cooling and heating unit 30, the secondary cooling and heating unit 60, and the tertiary cooling and heating unit 80.
And the liquid sulfur pool 90 is used for receiving the elemental sulfur output by the first-stage cold and hot unit 30, the second-stage cold and hot unit 60 and the third-stage cold and hot unit 80, degassing the elemental sulfur and storing the degassed elemental sulfur.
With continued reference to fig. 1, the outlet of the combustion unit 10 is in communication with the primary cold and heat unit 30 and the primary reaction unit 40, respectively, through the first bypass valve 20.
With continued reference to fig. 2, the combustion unit 10 includes a furnace 101 and a waste heat boiler 102.
Wherein, a feed inlet is provided at one side of the combustion furnace 101 for inputting fuel gas, air and acid gas.
The feed inlet is used for being communicated with a main fan and a desulfurization device respectively, the main fan is used for inputting fuel gas and air to the feed inlet, the desulfurization device is used for inputting acid gas to the feed inlet, and the acid gas comprises hydrogen sulfide gas.
Wherein, the feed inlet is a furnace end, and fuel gas, air and acid gas enter the combustion furnace 101 through the furnace end.
With continued reference to fig. 2, the outlet of the furnace 101 is in communication with the inlet of the waste heat boiler 102, and the outlet of the waste heat boiler 102 is in communication with the primary cold and heat unit 30 and the primary reaction unit 40 through the first bypass valve 20, respectively.
And the combustion furnace 101 is used for combusting the fuel gas and the air to generate inert flue gas under the condition that the first bypass valve 20 and the second bypass valve 50 are opened, and inputting the inert flue gas into the waste heat boiler 102.
The exhaust-heat boiler 102 is configured to receive the inert flue gas, stabilize the temperature of the inert flue gas, and enable the inert flue gas to sequentially pass through the first bypass valve 20, the first-stage reaction unit 40, the second bypass valve 50, and the second-stage reaction unit 70, so as to heat the first-stage catalyst bed layer and the second-stage catalyst bed layer.
The first bypass valve 20 and the second bypass valve 50 are both thermal bypass valves, which can withstand higher temperatures and have good heat resistance.
Wherein, a burner is arranged in the combustion furnace 101, and the burner is used for burning fuel gas and air to generate inert flue gas. The fuel gas and air are combusted in equivalent to release a large amount of heat, and the produced inert flue gas is high-temperature gas.
Wherein, the feed inlet of the combustion furnace 101 is also used for inputting temperature-adjusting steam, and the temperature-adjusting steam is low-temperature steam; since the inert flue gas is a high temperature gas, the temperature-adjusting steam is used to reduce the temperature of the inert flue gas to protect the burners in the furnace 101 from damage at high temperatures.
The exhaust-heat boiler 102 is used for cooling the inert flue gas to a certain temperature, so that the temperature of the inert flue gas is stable.
The inert flue gas is generated by combustion of fuel gas and air, does not participate in reaction, and is used as high-temperature gas to heat the first-stage catalyst bed layer and the second-stage catalyst bed layer.
The combustion furnace 101 is further configured to combust the fuel gas with air and react the acid gas with air to generate a process gas, and to input the process gas to the waste heat boiler 102, with the first bypass valve 20 and the second bypass valve 50 closed. The exhaust-heat boiler 102 is used for receiving the process gas, stabilizing the temperature of the process gas and enabling the process gas to sequentially pass through the primary cooling and heating unit 30, the primary reaction unit 40, the secondary cooling and heating unit 60, the secondary reaction unit 70 and the tertiary cooling and heating unit 80.
Wherein, the fuel gas and air are combusted equivalently to generate inert flue gas through a burner in the combustion furnace 101, the ratio of the acid gas and the air is controlled, one third of hydrogen sulfide in the acid gas and oxygen in the air are combusted to generate sulfur dioxide, and the remaining two thirds of hydrogen sulfide in the acid gas and the generated sulfur dioxide generate a Claus reaction to generate gaseous elemental sulfur.
Wherein, the combustion of fuel gas and air, the combustion of acid gas and air all give off a large amount of heat, and the process gas that produces is high temperature gas. The process gas comprises generated elemental sulfur, water vapor and inert flue gas, and various gases such as incompletely reacted hydrogen sulfide, sulfur dioxide, air, fuel gas and the like.
Wherein, the exhaust-heat boiler 102 is used for cooling the process gas to a certain temperature, so that the temperature of the process gas is stable.
Wherein, the feed inlet of the combustion furnace 101 is also used for inputting nitrogen gas under the condition that the nitrogen gas meets the requirements in the process of refining natural gas; the nitrogen does not participate in the reaction and is used for increasing the flow and heat of the inert flue gas and the process gas.
With continued reference to fig. 1, the inlet and outlet of the primary cold and heat unit 30 are in communication with the combustion unit 10 and the primary reaction unit 40, respectively.
With continued reference to fig. 2, the primary cold and hot unit 30 includes a primary condenser 301 and a primary reheat furnace 302.
The feed inlet of the first-stage condenser 301 is communicated with the discharge outlet of the combustion unit 10, the discharge outlet of the first-stage condenser 301 is communicated with the first feed inlet of the first-stage reheating furnace 302, and the discharge outlet of the first-stage reheating furnace 302 is communicated with the feed inlet of the first-stage reaction unit 40.
Wherein, the feed inlet of the primary condenser 301 is communicated with the discharge outlet of the waste heat boiler 102.
The primary condenser 301 is configured to condense the process gas, separate out elemental sulfur, and input the process gas from which elemental sulfur is separated out into the primary reheating furnace 302. The primary reheating furnace 302 is configured to receive the process gas, heat the process gas, and input the heated process gas to the primary reaction unit 40.
Wherein, the discharge port of the first-stage condenser 301 is also communicated with the liquid sulfur pool 90, and the first-stage condenser 301 is used for inputting the separated elemental sulfur into the liquid sulfur pool 90. After elemental sulfur is precipitated in the first-stage condenser 301, the content of elemental sulfur in the process gas is reduced.
With continued reference to fig. 2, a second inlet is also provided at one side of the primary reheating furnace 302, and the second inlet is used for inputting combustion gas and air. The primary reheat furnace 302 is used to combust fuel gas with air to heat the process gas.
Wherein, the fuel gas and air are combusted to generate inert flue gas, and a large amount of heat is released to heat the process gas.
With continued reference to fig. 1, the inlet ports of the primary reaction unit 40 are respectively communicated with the primary cold and hot unit 30 and the combustion unit 10 through the first bypass valve 20, and the outlet port of the primary reaction unit 40 is respectively communicated with the secondary cold and hot unit 60 and the secondary reaction unit 70 through the second bypass valve 50.
Wherein, the first-stage reaction unit 40 comprises a first-stage claus reactor 401, and a first-stage catalyst bed layer is arranged inside the first-stage claus reactor 401.
Wherein, the feed inlet of the first-stage claus reactor 401 is respectively communicated with the first-stage reheating furnace 302 and the waste heat boiler 102 through the first bypass valve 20, and the discharge outlet of the first-stage claus reactor 401 is respectively communicated with the second-stage cold and heat unit 60 and the second-stage reaction unit 70 through the second bypass valve 50.
The primary claus reactor 401 is configured to receive the inert flue gas to heat the primary catalyst bed layer when the first bypass valve 20 and the second bypass valve 50 are opened, and to input the inert flue gas into the secondary reaction unit 70 through the second bypass valve 50.
The primary claus reactor 401 is further configured to receive the process gas output by the primary reheating furnace 302 when the first bypass valve 20 and the second bypass valve 50 are closed, so that the heated process gas undergoes claus reaction on the heated primary catalyst bed to generate elemental sulfur, and the process gas is input to the secondary cooling and heating unit 60.
Wherein, the process gas heated by the primary reheating furnace 302 meets the temperature requirement of the primary Claus reactor 401, and the hydrogen sulfide and sulfur dioxide in the process gas are subjected to Claus reaction on the primary catalyst bed layer in the primary Claus reactor 401 to generate elemental sulfur; after the process gas produces elemental sulfur in the first stage claus reactor 401, the hydrogen sulfide and sulfur dioxide content of the process gas is reduced.
With continued reference to fig. 1, the inlet and outlet of the secondary cooling and heating unit 60 are in communication with the primary reaction unit 40 and the secondary reaction unit 70, respectively.
With continued reference to fig. 2, the secondary cold and hot unit 60 includes a secondary condenser 601 and a secondary reheat furnace 602. The feed inlet of the secondary condenser 601 is communicated with the discharge outlet of the primary reaction unit 40, the discharge outlet of the secondary condenser 601 is communicated with the first feed inlet of the secondary reheating furnace 602, and the discharge outlet of the secondary reheating furnace 602 is communicated with the feed inlet of the secondary reaction unit 70.
Wherein, the feed inlet of the secondary condenser 601 is communicated with the discharge outlet of the primary claus reactor 401.
The secondary condenser 601 is configured to condense the process gas, precipitate elemental sulfur, and input the process gas from which elemental sulfur is precipitated into the secondary reheating furnace 602. The secondary reheating furnace 602 is configured to receive the process gas, heat the process gas, and input the heated process gas to the secondary reaction unit 70.
Wherein, the discharge gate of second grade condenser 601 still communicates with liquid sulphur pond 90, and second grade condenser 601 is used for inputing the simple substance sulphur that separates out into liquid sulphur pond 90. After elemental sulfur is precipitated from the secondary condenser 601, the content of elemental sulfur in the process gas is reduced.
With continued reference to FIG. 2, a second inlet port is provided on one side of the secondary reheat furnace 602 for the input of fuel gas and air. A secondary reheat furnace 602 is used to combust fuel gas with air to heat the process gas.
Wherein, the fuel gas and air are combusted to generate inert flue gas, and a large amount of heat is released to heat the process gas.
With continued reference to fig. 1, the inlet ports of the secondary reaction unit 70 are respectively communicated with the secondary cooling and heating unit 60 and the primary reaction unit 40 through the second bypass valve 50, and the outlet port of the secondary reaction unit 70 is communicated with the tertiary cooling and heating unit 80.
Wherein the secondary reaction unit 70 comprises a secondary claus reactor 701, and a secondary catalyst bed is arranged inside the secondary claus reactor 701.
Wherein, the feed inlet of the secondary claus reactor 701 is respectively communicated with the secondary reheating furnace 602 and the primary claus reactor 401 through the second bypass valve 50, and the discharge outlet of the secondary claus reactor 701 is communicated with the tertiary cooling and heating unit 80.
The second-stage claus reactor 701 is configured to receive the inert flue gas when the first bypass valve 20 and the second bypass valve 50 are opened, to heat the second-stage catalyst bed, and to input the inert flue gas into the third-stage cooling and heating unit 80.
The second-stage claus reactor 701 is further configured to receive the process gas output by the second-stage reheating furnace 602 when the first bypass valve 20 and the second bypass valve 50 are closed, perform a claus reaction on the heated process gas on the second-stage catalyst bed to generate elemental sulfur, and input the process gas into the third-stage cooling and heating unit 80.
Wherein, the process gas heated by the secondary reheating furnace 602 meets the temperature requirement of the secondary Claus reactor 701, and the hydrogen sulfide and sulfur dioxide in the process gas are subjected to Claus reaction on a secondary catalyst bed layer in the secondary Claus reactor 701 to generate elemental sulfur; after the process gas generates elemental sulfur in the secondary claus reactor 701, the hydrogen sulfide and sulfur dioxide content of the process gas is reduced.
With continued reference to fig. 1, the feed inlet of the tertiary cold and hot unit 80 is in communication with the secondary reaction unit 70.
With continued reference to fig. 2, the three stage chiller-heater unit 80 includes a three stage condenser 801 and an off-gas trap 802. The feed inlet of the third-stage condenser 801 is communicated with the discharge outlet of the second-stage reaction unit 70, and the discharge outlet of the third-stage condenser 801 is communicated with the feed inlet of the tail gas catcher 802.
Wherein, the feed inlet of the third-stage condenser 801 is communicated with the discharge outlet of the second-stage Claus reactor 701.
And the third-stage condenser 801 is used for condensing the process gas, precipitating elemental sulfur, and inputting the process gas precipitated elemental sulfur into the tail gas catcher 802.
The discharge port of the third-stage condenser 801 is also communicated with the liquid sulfur pool 90, and the third-stage condenser 801 is used for inputting separated elemental sulfur into the liquid sulfur pool 90.
The tail gas collector 802 is configured to receive the process gas, heat the process gas, collect elemental sulfur in the process gas, and output a tail gas in the process gas.
Wherein, the discharge port of the tail gas catcher 802 is communicated with the liquid sulfur pool 90, and is used for inputting the caught elemental sulfur into the liquid sulfur pool 90.
After the tail gas catcher 802 heats the process gas, the elemental sulfur in the process gas is vaporized into elemental sulfur vapor, and after the tail gas catcher 802 catches the elemental sulfur vapor in the process gas, the elemental sulfur vapor is liquefied into liquid elemental sulfur, which is input into the liquid sulfur tank 90.
Wherein, the device still includes tail gas incinerator, and tail gas incinerator's feed inlet and tail gas trap 802's discharge gate intercommunication. And the tail gas incinerator is used for receiving the tail gas output by the tail gas catcher 802 and incinerating the tail gas.
The tail gas catcher 802 catches elemental sulfur in the process gas, and then inputs the remaining tail gas into the tail gas incinerator.
With continued reference to fig. 2, the apparatus further comprises a second gate valve 100, the second gate valve 100 being adapted to communicate the off-gas incinerator with an off-gas trap 802.
In another possible implementation manner, the device further comprises a tail gas treatment furnace, and a feed inlet of the tail gas treatment furnace is communicated with a discharge outlet of the tail gas trap 802. And the tail gas treatment furnace is used for receiving the tail gas output by the tail gas catcher 802 and treating the tail gas.
The working principle of the sulfur recovery device provided by the embodiment of the application is as follows:
during the operation of the sulfur recovery device, when the temperature of the first-stage catalyst bed layer and the second-stage catalyst bed layer needs to be raised to meet the temperature condition of the acid gas reaction, the first bypass valve 20 and the second bypass valve 50 are in an open state.
Wherein, the inert flue gas generated by the combustion unit 10 passes through the first bypass valve 20 and enters the first-stage claus reactor 401 to heat the first-stage catalyst bed layer. The inert flue gas passes out of the first-stage claus reactor 401, then passes through the second bypass valve 50, enters the second-stage claus reactor 701, and heats the second-stage catalyst bed. Therefore, the condition that the temperature of the inert flue gas is raised after the inert flue gas is cooled is avoided, the time for raising the temperature of the first-stage catalyst bed layer and the second-stage catalyst bed layer is shortened, and the time of the sulfur recovery device during working is saved.
When high-temperature gas is required to heat the catalyst bed to vaporize and remove elemental sulfur on the catalyst bed during the non-operation period of the sulfur recovery device, the first bypass valve 20 and the second bypass valve 50 are in an open state.
High-temperature inert flue gas produced by the combustion unit 10 passes through the first bypass valve 20 and enters the first-stage Claus reactor 401, and the temperature of the first-stage catalyst bed is raised, so that elemental sulfur deposited in gaps of the first-stage catalyst bed is vaporized and removed. The vaporized and removed elemental sulfur enters the secondary claus reactor 701 along with the high-temperature inert flue gas, and the temperature of the secondary catalyst bed is raised, so that the elemental sulfur attached to the pores of the secondary catalyst bed is vaporized and removed. The vaporized and removed elemental sulfur enters the third-stage cooling and heating unit 80 along with the high-temperature inert flue gas, and the inert flue gas is condensed by the third-stage cooling and heating unit 80 to separate out elemental sulfur. Therefore, the condition that the temperature of the inert flue gas is raised after the inert flue gas is cooled is avoided, the time for vaporizing and removing the elemental sulfur deposited on the first-stage catalyst bed layer and the second-stage catalyst bed layer is shortened, and the time of the sulfur recovery device in the non-working period is saved. Therefore, after the elemental sulfur deposited on the first-stage catalyst bed layer and the second-stage catalyst bed layer is vaporized and removed, the safety of the sulfur recovery device during maintenance can be met, and the efficient operation of the sulfur recovery device is guaranteed.
The embodiment of the application provides a sulfur recovery device, the device is through setting up first bypass valve 20 and second bypass valve 50, the inertia flue gas that makes combustion unit 10 produce can pass one-level reaction unit 40 and second grade reaction unit 70 in proper order, heat up one-level catalyst bed and second grade catalyst bed respectively, avoided raising the temperature again after cooling inert flue gas, labour saving and time saving, and then improved the efficiency that heaies up one-level catalyst bed and second grade catalyst bed, thereby the efficiency of elemental sulfur recovery has been improved.
The embodiment of the application provides a sulfur recovery method, which is applied to the device and takes the reference of fig. 3, and the method comprises the following steps:
step 301: the first bypass valve 20 and the second bypass valve 50 are opened.
Step 302: and controlling the combustion unit 10 to combust the fuel gas and air to generate inert flue gas, wherein the inert flue gas sequentially passes through the first bypass valve 20, the first-stage reaction unit 40, the second bypass valve 50 and the second-stage reaction unit 70 so as to heat a first-stage catalyst bed layer in the first-stage reaction unit 40 and a second-stage catalyst bed layer in the second-stage reaction unit 70.
Step 303: the first bypass valve 20 and the second bypass valve 50 are closed.
Step 304: the combustion unit 10 is controlled to combust the fuel gas with air and the acid gas with air to generate the process gas, and the process gas sequentially passes through the primary cooling and heating unit 30, the primary reaction unit 40, the secondary cooling and heating unit 60, the secondary reaction unit 70 and the tertiary cooling and heating unit 80.
Step 305: the first-stage cooling and heating unit 30, the second-stage cooling and heating unit 60 and the third-stage cooling and heating unit 80 are controlled to condense the process gas, separate out elemental sulfur, and heat the process gas and then output the process gas.
Step 306: the first-stage reaction unit 40 and the second-stage unit are controlled to make the heated process gas respectively perform the Claus reaction in the first-stage catalyst bed layer and the second-stage catalyst bed layer which are heated to generate elemental sulfur.
Step 307: the first bypass valve 20 and the second bypass valve 50 are opened.
Step 308: and controlling the combustion unit 10 to enable the fuel gas and the air to be combusted to generate inert flue gas, wherein the inert flue gas sequentially passes through the first bypass valve 20, the first-stage reaction unit 40, the second bypass valve 50 and the second-stage reaction unit 70 to heat the first-stage catalyst bed layer and the second-stage catalyst bed layer, so that elemental sulfur on the first-stage catalyst bed layer and the second-stage catalyst bed layer is vaporized and removed.
The embodiment of the application provides a sulfur recovery method, and the method enables inert flue gas generated by a combustion unit 10 to sequentially pass through a first-stage reaction unit 40 and a second-stage reaction unit 70 through a first bypass valve 20 and a second bypass valve 50, and heats a first-stage catalyst bed layer and a second-stage catalyst bed layer respectively, so that the inert flue gas is prevented from being cooled and then heated, time and labor are saved, the efficiency of heating the first-stage catalyst bed layer and the second-stage catalyst bed layer is improved, and the efficiency of recovering elemental sulfur is improved.
The above description is only exemplary of the present application and should not be taken as limiting, as any modification, equivalent replacement, or improvement made within the spirit and principle of the present application should be included in the protection scope of the present application.
Claims (10)
1. The sulfur recovery device is characterized by comprising a combustion unit (10), a first bypass valve (20), a first-stage cold and hot unit (30), a first-stage reaction unit (40), a second bypass valve (50), a second-stage cold and hot unit (60), a second-stage reaction unit (70) and a third-stage cold and hot unit (80);
the combustion unit (10), the primary cooling and heating unit (30), the primary reaction unit (40), the secondary cooling and heating unit (60), the secondary reaction unit (70) and the tertiary cooling and heating unit (80) are communicated in sequence;
a feed inlet is formed in one side of the combustion unit (10) and used for inputting fuel gas, air and acid gas;
the discharge hole of the combustion unit (10) is also communicated with the feed hole of the primary reaction unit (40) through the first bypass valve (20), and the discharge hole of the primary reaction unit (40) is also communicated with the feed hole of the secondary reaction unit (70) through the second bypass valve (50);
the combustion unit (10) is used for combusting the fuel gas and the air to generate inert flue gas under the condition that the first bypass valve (20) and the second bypass valve (50) are opened, and the inert flue gas sequentially passes through the first bypass valve (20), the primary reaction unit (40), the second bypass valve (50) and the secondary reaction unit (70) so as to heat a primary catalyst bed layer in the primary reaction unit (40) and a secondary catalyst bed layer in the secondary reaction unit (70);
the combustion unit (10) is further used for combusting the fuel gas and the air and reacting the acid gas and the air to generate a process gas under the condition that the first bypass valve (20) and the second bypass valve (50) are closed, and the process gas sequentially passes through the primary cold and hot unit (30), the primary reaction unit (40), the secondary cold and hot unit (60), the secondary reaction unit (70) and the tertiary cold and hot unit (80);
the primary cooling and heating unit (30), the secondary cooling and heating unit (60) and the tertiary cooling and heating unit (80) are used for condensing the process gas, separating out elemental sulfur, heating the process gas and outputting the heated process gas;
the first-stage reaction unit (40) and the second-stage unit are used for enabling the heated process gas to respectively carry out Claus reaction on the first-stage catalyst bed layer and the second-stage catalyst bed layer which are heated to generate elemental sulfur.
2. A sulphur recovery unit according to claim 1, wherein the combustion unit (10) comprises a combustion furnace (101) and a waste heat boiler (102);
a feed inlet is formed in one side of the combustion furnace (101) and used for inputting the fuel gas, the air and the acid gas;
the discharge hole of the combustion furnace (101) is communicated with the feed hole of the waste heat boiler (102), and the discharge hole of the waste heat boiler (102) is respectively communicated with the primary cold and hot unit (30) and the primary reaction unit (40) through the first bypass valve (20);
the combustion furnace (101) is used for combusting the fuel gas and the air to generate inert flue gas under the condition that the first bypass valve (20) and the second bypass valve (50) are opened, and the inert flue gas is input into the waste heat boiler (102);
the waste heat boiler (102) is configured to receive the inert flue gas, and after the inert flue gas is stabilized in temperature, the inert flue gas sequentially passes through the first bypass valve (20), the first-stage reaction unit (40), the second bypass valve (50), and the second-stage reaction unit (70) to heat the first-stage catalyst bed layer and the second-stage catalyst bed layer;
the combustion furnace (101) is further used for combusting the fuel gas and the air and reacting the acid gas and the air to generate a process gas under the condition that the first bypass valve (20) and the second bypass valve (50) are closed, and the process gas is input into the waste heat boiler (102);
the waste heat boiler (102) is used for receiving the process gas, and after the process gas is subjected to temperature stabilization, the process gas sequentially passes through the primary cold and hot unit (30), the primary reaction unit (40), the secondary cold and hot unit (60), the secondary reaction unit (70) and the tertiary cold and hot unit (80).
3. A sulphur recovery unit according to claim 1, wherein the primary cooling and heating unit (30) comprises a primary condenser (301) and a primary reheat furnace (302);
the feeding hole of the primary condenser (301) is communicated with the discharging hole of the combustion unit (10), the discharging hole of the primary condenser (301) is communicated with the first feeding hole of the primary reheating furnace (302), and the discharging hole of the primary reheating furnace (302) is communicated with the feeding hole of the primary reaction unit (40);
the primary condenser (301) is used for condensing the process gas, precipitating the elemental sulfur, and inputting the process gas with the precipitated elemental sulfur into the primary reheating furnace (302);
the primary reheating furnace (302) is used for receiving the process gas, heating the process gas and inputting the heated process gas into the primary reaction unit (40).
4. A sulfur recovery device according to claim 3, wherein a second inlet is provided at one side of the primary reheating furnace (302), and the second inlet is used for inputting combustion gas and air;
the primary reheat furnace (302) is configured to combust the fuel gas with the air to heat the process gas.
5. A sulphur recovery unit according to claim 1, wherein the secondary cooling and heating unit (60) comprises a secondary condenser (601) and a secondary reheat furnace (602);
the feeding hole of the secondary condenser (601) is communicated with the discharging hole of the primary reaction unit (40), the discharging hole of the secondary condenser (601) is communicated with the first feeding hole of the secondary reheating furnace (602), and the discharging hole of the secondary reheating furnace (602) is communicated with the feeding hole of the secondary reaction unit (70);
the secondary condenser (601) is used for condensing the process gas, precipitating the elemental sulfur, and inputting the process gas with the precipitated elemental sulfur into the secondary reheating furnace (602);
the secondary reheating furnace (602) is used for receiving the process gas, heating the process gas and inputting the heated process gas into the secondary reaction unit (70).
6. A sulphur recovery unit according to claim 5, wherein the secondary reheating furnace (602) is further provided with a second inlet for the input of fuel gas and air;
the secondary reheat furnace (602) is configured to combust the fuel gas with the air to heat the process gas.
7. A sulphur recovery unit according to claim 1, wherein the tertiary cold and hot unit (80) comprises a tertiary condenser (801) and an off-gas trap (802);
the feed inlet of the third-stage condenser (801) is communicated with the discharge outlet of the second-stage reaction unit (70), and the discharge outlet of the third-stage condenser (801) is communicated with the feed inlet of the tail gas catcher (802);
the three-stage condenser (801) is used for condensing the process gas, precipitating the elemental sulfur, and inputting the process gas with the precipitated elemental sulfur into the tail gas catcher (802);
the tail gas catcher (802) is used for receiving the process gas, catching elemental sulfur in the process gas after heating the process gas, and outputting tail gas in the process gas.
8. The sulphur recovery device according to claim 7, further comprising a tail gas incinerator, the feed inlet of which is in communication with the discharge outlet of the tail gas trap (802);
the tail gas incinerator is used for receiving the tail gas output by the tail gas catcher (802) and incinerating the tail gas.
9. The sulfur recovery device according to claim 1, further comprising a liquid sulfur pool (90), wherein the liquid sulfur pool (90) is respectively communicated with the discharge ports of the primary cold and hot unit (30), the secondary cold and hot unit (60) and the tertiary cold and hot unit (80);
the liquid sulfur pool (90) is used for receiving the elemental sulfur output by the primary cooling and heating unit (30), the secondary cooling and heating unit (60) and the tertiary cooling and heating unit (80), degassing the elemental sulfur and storing the degassed elemental sulfur.
10. A sulphur recovery process, for use in an apparatus according to any one of claims 1 to 9, the process comprising:
opening the first bypass valve (20) and the second bypass valve (50);
controlling the combustion unit (10) to combust the fuel gas with the air to generate inert flue gas, wherein the inert flue gas sequentially passes through the first bypass valve (20), the primary reaction unit (40), the second bypass valve (50) and the secondary reaction unit (70) to heat a primary catalyst bed layer in the primary reaction unit (40) and a secondary catalyst bed layer in the secondary reaction unit (70);
closing the first bypass valve (20) and the second bypass valve (50);
controlling the combustion unit (10) to enable the fuel gas to be combusted with the air and the acid gas to be reacted with the air to generate a process gas, and enabling the process gas to sequentially pass through the primary cooling and heating unit (30), the primary reaction unit (40), the secondary cooling and heating unit (60), the secondary reaction unit (70) and the tertiary cooling and heating unit (80);
controlling the primary cooling and heating unit (30), the secondary cooling and heating unit (60) and the tertiary cooling and heating unit (80), condensing the process gas, separating out elemental sulfur, and heating the process gas for output;
controlling the primary reaction unit (40) and the secondary unit to enable the heated process gas to respectively carry out Claus reaction in the heated primary catalyst bed layer and the heated secondary catalyst bed layer to generate elemental sulfur;
opening the first bypass valve (20) and the second bypass valve (50);
and controlling the combustion unit (10) to combust the fuel gas with the air to generate inert flue gas, wherein the inert flue gas sequentially passes through the first bypass valve (20), the first-stage reaction unit (40), the second bypass valve (50) and the second-stage reaction unit (70) to heat the first-stage catalyst bed layer and the second-stage catalyst bed layer, so that elemental sulfur on the first-stage catalyst bed layer and the second-stage catalyst bed layer is vaporized and removed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110505682.1A CN115321489B (en) | 2021-05-10 | Sulfur recovery device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110505682.1A CN115321489B (en) | 2021-05-10 | Sulfur recovery device and method |
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| Publication Number | Publication Date |
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| CN115321489A true CN115321489A (en) | 2022-11-11 |
| CN115321489B CN115321489B (en) | 2024-06-25 |
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| CN101117214A (en) * | 2007-04-30 | 2008-02-06 | 中国石油集团工程设计有限责任公司 | Improved low-temperature Claus sulfur recovery method |
| CN201052968Y (en) * | 2007-03-08 | 2008-04-30 | 四川四维工程设计有限公司 | Low-temperature Claus sulfur reclaiming device |
| CN206447572U (en) * | 2017-01-05 | 2017-08-29 | 中国石油化工股份有限公司 | Hot nitrogen purges sulfur recovery facility |
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| RU2221742C2 (en) * | 2002-02-08 | 2004-01-20 | Открытое акционерное общество "Институт Гипроникель" | Method for production of elementary sulfur from emission gases containing sulfur dioxide |
| CN201052968Y (en) * | 2007-03-08 | 2008-04-30 | 四川四维工程设计有限公司 | Low-temperature Claus sulfur reclaiming device |
| CN101117214A (en) * | 2007-04-30 | 2008-02-06 | 中国石油集团工程设计有限责任公司 | Improved low-temperature Claus sulfur recovery method |
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