CN216711600U - Containing H2S synthetic gas low-temperature chemical-looping desulfurization and sulfuric acid co-production system - Google Patents
Containing H2S synthetic gas low-temperature chemical-looping desulfurization and sulfuric acid co-production system Download PDFInfo
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- CN216711600U CN216711600U CN202123174328.XU CN202123174328U CN216711600U CN 216711600 U CN216711600 U CN 216711600U CN 202123174328 U CN202123174328 U CN 202123174328U CN 216711600 U CN216711600 U CN 216711600U
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- fuel reactor
- desulfurization
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 16
- 230000023556 desulfurization Effects 0.000 title claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 239000000446 fuel Substances 0.000 claims abstract description 41
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 27
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 27
- 238000010521 absorption reaction Methods 0.000 claims abstract description 23
- 239000000126 substance Substances 0.000 claims abstract description 9
- 239000002253 acid Substances 0.000 claims abstract description 8
- 239000003054 catalyst Substances 0.000 claims abstract description 8
- 230000003197 catalytic effect Effects 0.000 claims abstract description 8
- 238000009826 distribution Methods 0.000 claims description 17
- 230000005587 bubbling Effects 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 19
- 229910052717 sulfur Inorganic materials 0.000 abstract description 11
- 239000011593 sulfur Substances 0.000 abstract description 11
- 239000000463 material Substances 0.000 abstract description 7
- 239000007789 gas Substances 0.000 description 45
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 22
- 229910052760 oxygen Inorganic materials 0.000 description 22
- 239000001301 oxygen Substances 0.000 description 22
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 16
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 13
- 238000000034 method Methods 0.000 description 13
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 12
- 238000007254 oxidation reaction Methods 0.000 description 9
- 238000002485 combustion reaction Methods 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 239000000969 carrier Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 239000002341 toxic gas Substances 0.000 description 1
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- Industrial Gases (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model provides a catalyst containing H2The system for S synthesis gas low-temperature chemical-looping desulfurization and sulfuric acid co-production comprises a chemical-looping reaction unit, SO2To SO3Catalytic conversion unit, SO3An absorption acid making unit; the chemical chain reaction unit comprises an air reactor, a fuel reactor, a cyclone separator and a condenser; the SO2To SO3The catalytic conversion unit comprises a contact chamber; the SO3The absorption acid-making unit comprises absorptionA tower; the air reactor is connected with the cyclone separator through a lifting pipe, a discharge pipe at the lower part of the cyclone separator is connected with the lower part of the fuel reactor, an airflow outlet of the cyclone separator is connected with an inlet of the contact chamber, an outlet of the contact chamber is connected with an inlet of the absorption tower through a pipeline, the bottom of the fuel reactor is connected with the air reactor through a material returning device, and an outlet of the fuel reactor is connected with a condenser. The utility model realizes the resource utilization of sulfur while ensuring that the quality of the synthesis gas is not reduced.
Description
Technical Field
The utility model belongs to the technical field of synthesis gas purification, and particularly relates to a catalyst containing H2S synthetic gas low-temperature chemical chain desulfurization and sulfuric acid coproduction system.
Background
Most primary energy sources contain elemental sulfur. The synthesis gas produced by energy conversion processes (e.g., gasification, reforming, fermentation, etc.) contains hydrogen sulfide (H) at a certain concentration2S) gas. H2S is a toxic gas with pungent odor, and has significant harm to equipment, human bodies and the environment. To prevent H2S gas affects equipment, products and the like in the process of deep energy conversion and resource utilization of synthesis gas, and the synthesis gas firstly needs to react with H2And removing the S gas. Under the premise of not influencing the quality of the synthesis gas, the H is added2Oxidation of S to sulfur dioxide (SO)2) SO produced2The deep conversion into sulfuric acid is one of the technical choices for resource utilization.
At present, H of industrial process2The technical route for preparing sulfuric acid from S mainly comprises the following steps: h2Oxidation of S and air, SO2To SO3Catalytic conversion and subsequent SO3Absorbing the acid making process. SO (SO)2To SO3Catalytic conversion and subsequent SO3The process of absorbing and preparing acid is relatively mature. H for the first step2S oxidation process, the traditional technique mostly adopts air as an oxidation medium, H2S and oxygen in the air are combusted in the combustion furnace to generate SO2. In the combustion furnace, when H2When the concentration of S is low, the S needs to be supported by combustible gas, namely H2S the combustion process provides a heat source. The temperature in the combustion furnace reaches thousands of degrees in the traditional process, H2S is contacted with oxygen and is easy to explode; meanwhile, the combustion supporting of the combustible gas consumes the high-quality combustible gas, which causes the waste of energy.
Construction of novel H-containing2System and method for S synthesis gas low-temperature chemical-looping desulfurization and sulfuric acid co-productionThe method realizes the desulfurization of the synthesis gas at low temperature and the resource utilization of the sulfur at the same time, and has wide social benefits and industrial prospects.
SUMMERY OF THE UTILITY MODEL
The technical problem is as follows: in order to overcome the conventional H2The problem of resource waste of high temperature and combustible gas in the S sulfuric acid preparation process is a technical problem to be solved how to realize resource utilization of sulfur while ensuring that the quality of synthesis gas is not reduced.
The technical scheme is as follows: the utility model provides a catalyst containing H2S synthetic gas low-temperature chemical chain desulfurization and sulfuric acid coproduction system.
Containing H of the utility model2The system for S synthesis gas low-temperature chemical-looping desulfurization and sulfuric acid co-production comprises a chemical-looping reaction unit, SO2To SO3Catalytic conversion unit, SO3An absorption acid making unit; the chemical chain reaction unit comprises an air reactor, a fuel reactor, a cyclone separator and a condenser; the SO2To SO3The catalytic conversion unit comprises a contact chamber; the SO3The absorption acid making unit comprises an absorption tower; the air reactor is connected with the cyclone separator through a lifting pipe, a lower discharging pipe of the cyclone separator is connected with the lower part of the fuel reactor, an airflow outlet of the cyclone separator is connected with an inlet of the contact chamber, an outlet of the contact chamber is connected with an inlet of the absorption tower through a pipeline, the bottom of the fuel reactor is connected with the air reactor through a material returning device, and an outlet of the fuel reactor is connected with a condenser.
Further, an air reactor air distribution plate is arranged at the inlet of the air reactor, a fuel reactor air distribution plate is arranged at the bottom of the fuel reactor, and the air reactor air distribution plate and the fuel reactor air distribution plate are air distribution partition plates with porous shapes or hood structures.
Further, the catalyst within the contacting chamber may be arranged in two or more layers.
Further, the fuel reactor is a bubbling fluidized bed.
Further, an air inlet is provided at one side of the contact chamber.
Has the advantages that:
1. the system and method of the utility model are applicable to H-containing2S synthesis gas purification and resource utilization of sulfur are realized. Containing H2S synthetic gas is oxidized into elemental sulfur by an oxygen carrier in a fuel reactor, partial elemental sulfur can be directly recycled, and sulfur loaded on the oxygen carrier in a liquid phase enters an air reactor to be oxidized into SO2SO formed2Entering a subsequent acid making system and being used for H2SO4And (4) preparation.
2. The fuel reactor has low operation temperature of 150-300 ℃ and oxygen carrier capable of oxidizing H only2S is elemental sulfur, the synthetic gas does not react with the oxygen carrier, and the quality of the synthetic gas is not influenced by materials and operating conditions in the fuel reactor. The sulfur resource is recycled and the function of purifying the synthesis gas is achieved.
Drawings
FIG. 1 is a schematic diagram of a chemical looping low temperature oxidation process;
FIG. 2 is a system flow diagram of the present invention;
fig. 3 is a system configuration diagram of the present invention.
The reference numerals in the figures represent the following:
1. a chemical-looping reactor unit; 2. SO (SO)2To SO3A catalytic conversion unit; 3. SO (SO)3And absorbing an acid making unit.
1-1. an air reactor; 1-2, a riser; 1-3. a cyclone separator; 1-4. a fuel reactor; 1-5, a material returning device; 1-6. air distribution plate of air reactor; 1-7, a discharge pipe; 1-8. air distribution plate of fuel reactor; 1-9. fuel reactor gas inlet; 1-10. air reactor gas inlet; 1-11. an airflow outlet of the cyclone separator; 1-12. fuel reactor outlet; 1-13. a condenser; 1-14. condenser outlet; 1-15, connecting the pipeline.
2-1. a contacting chamber; 2-2. contacting chamber inlet; 2-3. an air inlet; 2-4. a contact chamber outlet; 2-5, connecting the pipeline.
3-1, an absorption tower; 3-2, an absorption tower inlet; 3-3, a liquid outlet of the absorption tower; and 3-4, a tail gas outlet of the absorption tower.
Detailed Description
The present invention will be further described with reference to the accompanying drawings.
Example 1
The utility model relates to a catalyst containing H2The system for S synthesis gas low-temperature chemical-looping desulfurization and sulfuric acid co-production is shown in figure 2 and comprises a chemical-looping reactor unit 1, SO2To SO3Catalytic conversion unit 2 and SO3An absorption acid-making unit 3.
Further, as shown in FIG. 3, the chemical looping reaction unit 1 is a circulating bed material device composed of an air reactor 1-1, a riser 1-2, a cyclone separator 1-3, a fuel reactor 1-4 and a return feeder 1-5. The upper part of the air reactor 1-1 is communicated with a cyclone separator 1-3 through a riser 1-2; a J-shaped discharge pipe 1-7 at the lower part of the cyclone separator 1-3 is introduced into the lower part of the fuel reactor 1-4; the fuel reactor 1-4 is communicated with the air reactor 1-1 through a return feeder 1-5. The air distribution plate 1-6 of the air reactor is arranged at the inlet 1-10 of the air reactor, the air distribution plate 1-8 of the fuel reactor is arranged at the bottom 1-9 of the fuel reactor, and the air distribution plate 1-6 of the air reactor and the air distribution plate 1-8 of the fuel reactor are air distribution partition plates with porous shapes or air cap structures and are used for supporting bed materials.
The synthesis gas at the fuel reactor outlet 1-12 enters the condenser 1-13 and is discharged through the condenser outlet 1-14. An airflow outlet 1-11 of the cyclone separator is connected with an inlet 2-2 of the contact chamber through a connecting pipeline 1-15; the air reactor stream enters the contactor 2-1 from contactor inlet 2-2; SO (SO)2To SO3The air inlet 2-3 in the catalytic conversion unit 2 is used for assisting SO2To SO3A supplemental air inlet for catalytic conversion.
SO2To SO3The outlet 2-4 of the contact chamber of the catalytic conversion unit 2 is connected with the inlet 3-2 of the absorption tower through a connecting pipeline 2-5; the gas flow after catalytic conversion enters an absorption tower 3-1 from an inlet 3-2 of the absorption tower; the sulfuric acid liquid is discharged through a liquid outlet 3-3 of the absorption tower, and the tail gas is discharged through a tail gas outlet 3-4 of the absorption tower.
The catalyst in the contacting chamber in this embodiment may be arranged in two or more layers.
With the above-mentioned hydrogen-containing compounds2System for low-temperature chemical-looping desulfurization and sulfuric acid co-production of S synthetic gas to contain H2Method for low-temperature chemical-looping desulfurization and co-production of sulfuric acid from S synthesis gas containing H2The synthesis gas of the S enters a fuel reactor, and the function of purifying the synthesis gas is realized while the resource of sulfur is changed by the circulation of the circulating oxygen carrier in the device, and the specific method comprises the following steps:
and (3) synthetic gas purification reaction: the fuel reactor is a bubbling fluidized bed and contains H2S synthetic gas enters the bottom of the fuel reactor, and H is generated under the action of an oxygen carrier2S gas is oxidized into elemental sulfur by an oxygen carrier, part of the generated elemental sulfur is attached to the surface of the oxygen carrier in a liquid phase form, the other part of the generated elemental sulfur and synthesis gas are discharged out of a fuel reactor in a gas phase form, the elemental sulfur can be recycled after condensation by a condenser, and the synthesis gas is purified; at the same time, the oxygen carrier is reduced to a lower valence state.
Preparation of SO by oxidation2Reaction: the sulfur simple substance attached to the surface of the oxygen carrier circulates to the air reactor along with the oxygen carrier to be combusted, and the oxygen carrier and the sulfur are subjected to oxidation reaction to generate SO under the air atmosphere2. Meanwhile, the reduced oxygen carrier from the fuel reactor enters the air reactor through the material returning device to perform oxidation reaction with the air entering from the bottom, so that the regeneration of the oxygen carrier is realized. The oxygen carrier after oxidation regeneration enters a cyclone separator through a riser, and the separated flue gas contains SO2Is used to remove the oxygen-depleted flue gas.
SO2Catalytic conversion reaction: containing SO2The oxygen-poor flue gas enters SO2To SO3Catalytic conversion unit, SO under the action of catalyst2Conversion to SO3。
Absorption acid-making reaction: generated SO3Is absorbed into sulfuric acid in the absorption tower, thereby realizing resource conversion of sulfur.
The synthesis gas in the embodiment is CO and H2、CH4And so on.
H in the present example2The S inlet concentration range is as follows: 0 to Vol.100 percent.
Oxygen carrier described in the present embodimentComprises the following steps: can be combined with H2S is oxidized into all oxygen carriers of sulfur simple substance, and the components of the oxygen carriers comprise active substances and inert carriers. For example: v2O5/TiO2An oxygen carrier.
In the embodiment, the reaction temperature in the air reactor is 150-300 ℃; the reaction temperature in the fuel reactor is 150-300 ℃.
In this embodiment, the fluidizing gas at the bottom of the air reactor is: air; the fuel reactor adds reaction gas through the bottom: a synthesis gas comprising hydrogen sulphide.
The above examples are only preferred embodiments of the present invention, it should be noted that: the utility model can be applied to various fields of medical equipment, such as medical equipment, etc. without departing from the principle of the utility model.
Claims (5)
1. Containing H2The system for low-temperature chemical-looping desulfurization and co-production of sulfuric acid of S synthesis gas is characterized by comprising a chemical-looping reaction unit (1), SO2To SO3Catalytic conversion unit (2), SO3An absorption acid-making unit (3); the chemical chain reaction unit (1) comprises an air reactor (1-1), a fuel reactor (1-4), a cyclone separator (1-3) and a condenser (1-13); the SO2To SO3The catalytic conversion unit (2) comprises a contact chamber (2-1); the SO3The absorption acid making unit (3) comprises an absorption tower (3-1); the air reactor (1-1) is connected with the cyclone separator (1-3) through a lifting pipe (1-2), a lower discharging pipe 1-7 of the cyclone separator (1-3) is connected with the lower part of the fuel reactor (1-4), an airflow outlet (1-11) of the cyclone separator (1-3) is connected with an inlet (2-2) of the contact chamber, an outlet (2-4) of the contact chamber is connected with an inlet (3-2) of the absorption tower through a pipeline, the bottom of the fuel reactor (1-4) is connected with the air reactor (1-1) through a return feeder (1-5), and an outlet (1-12) of the fuel reactor is connected with a condenser (1-13).
2. The H-containing according to claim 12The system for low-temperature chemical-looping desulfurization and sulfuric acid coproduction of synthesis gas is characterized in that an air reactor air distribution plate (1-6) is arranged at an inlet of an air reactor (1-1), a fuel reactor air distribution plate (1-8) is arranged at the bottom of a fuel reactor (1-4), and the air reactor air distribution plate (1-6) and the fuel reactor air distribution plate (1-8) are air distribution partition plates with porous shapes or hood structures.
3. The H-containing according to claim 12The system for low-temperature chemical-looping desulfurization and sulfuric acid coproduction of the S synthesis gas is characterized in that catalysts in the contact chamber (2-1) are arranged in two or more layers.
4. The H-containing according to claim 12The system for low-temperature chemical-looping desulfurization and sulfuric acid co-production of the S synthesis gas is characterized in that the fuel reactor (1-4) is a bubbling fluidized bed.
5. The H-containing according to claim 12The system for S synthesis gas low-temperature chemical-looping desulfurization and sulfuric acid coproduction is characterized in that an air inlet (2-3) is formed in one side of the contact chamber (2-1).
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| CN202123174328.XU CN216711600U (en) | 2021-12-17 | 2021-12-17 | Containing H2S synthetic gas low-temperature chemical-looping desulfurization and sulfuric acid co-production system |
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|---|---|---|---|---|
| CN114031039A (en) * | 2021-12-17 | 2022-02-11 | 南京师范大学 | Containing H2System and method for S synthesis gas low-temperature chemical-looping desulfurization and sulfuric acid co-production |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114031039A (en) * | 2021-12-17 | 2022-02-11 | 南京师范大学 | Containing H2System and method for S synthesis gas low-temperature chemical-looping desulfurization and sulfuric acid co-production |
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