CN104528659A - Sulfur recycling process for circularly treating low-concentration acidy gas by utilizing liquid sulfur - Google Patents
Sulfur recycling process for circularly treating low-concentration acidy gas by utilizing liquid sulfur Download PDFInfo
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- CN104528659A CN104528659A CN201410788412.6A CN201410788412A CN104528659A CN 104528659 A CN104528659 A CN 104528659A CN 201410788412 A CN201410788412 A CN 201410788412A CN 104528659 A CN104528659 A CN 104528659A
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- Prior art keywords
- sulfur
- gas
- sour gas
- ammonia
- volumetric concentration
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 111
- 238000000034 method Methods 0.000 title claims abstract description 100
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 78
- 239000011593 sulfur Substances 0.000 title claims abstract description 78
- 239000007788 liquid Substances 0.000 title abstract description 4
- 238000004064 recycling Methods 0.000 title abstract 5
- 238000006243 chemical reaction Methods 0.000 claims abstract description 55
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 30
- 230000003647 oxidation Effects 0.000 claims abstract description 28
- 239000003245 coal Substances 0.000 claims abstract description 25
- 238000005406 washing Methods 0.000 claims abstract description 12
- 238000002485 combustion reaction Methods 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 81
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 62
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 52
- 229910021529 ammonia Inorganic materials 0.000 claims description 31
- 239000000126 substance Substances 0.000 claims description 24
- 238000011084 recovery Methods 0.000 claims description 20
- 238000005516 engineering process Methods 0.000 claims description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 16
- 238000005984 hydrogenation reaction Methods 0.000 claims description 12
- 238000005200 wet scrubbing Methods 0.000 claims description 12
- 239000005864 Sulphur Substances 0.000 claims description 11
- 239000002918 waste heat Substances 0.000 claims description 10
- 239000003513 alkali Substances 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 239000007800 oxidant agent Substances 0.000 claims description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical group O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 238000000889 atomisation Methods 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- DWNBOPVKNPVNQG-LURJTMIESA-N (2s)-4-hydroxy-2-(propylamino)butanoic acid Chemical compound CCCN[C@H](C(O)=O)CCO DWNBOPVKNPVNQG-LURJTMIESA-N 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 2
- 239000012535 impurity Substances 0.000 abstract description 6
- 238000002156 mixing Methods 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 4
- 238000001311 chemical methods and process Methods 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 230000002378 acidificating effect Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005422 blasting Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
- C01B17/0495—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by dissociation of hydrogen sulfide into the elements
-
- 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
- C01B17/0408—Pretreatment of the hydrogen sulfide containing gases
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a sulfur recycling process for circularly treating low-concentration acidy gas by utilizing liquid sulfur. The sulfur recycling process is characterized by comprising the following steps: mixing atomized liquid sulfur with a H2S acidy gas generated in a coal chemical process, performing Claus combustion by adopting rich oxidation combustion-supporting or air combustion-supporting, performing two-stage Claus reaction on process gas generated in combustion, performing hydrogenation-direct oxidization and wet-process washing on a tail gas generated by the two-stage Claus reaction in sequence, recycling the sulfur produced in the Claus combustion process, the two-stage Claus reaction process and the hydrogenation-direct oxidization process. The sulfur recycling process can be used for guaranteeing the combustion temperature of the raw material acidy gas with a low heat value, and also can be used for decomposing harmful impurities in the raw material acidy gas.
Description
Technical field
The present invention relates to a kind of recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas, for sulfur recovery facility design, belong to sulphur recovery field.
Background technology
For the various lower concentration Acidic Gas Treating that Coal Chemical Industry process produces, generally containing H
2s concentration is on the low side, and the sour gas come as low-temperature rectisol workshop section contains CO
2height, H
2s concentration about 25%, and containing a small amount of methyl alcohol, and the sour gas that phenol recovery ammonia workshop section comes is containing NH
3, containing H
2o, H
2s concentration about 4%, because the calorific value of these sour gas is very low, even allocate pure oxygen into also cannot reach burning ammonia temperature, the claus process of shunting also cannot process.
Current process H
2the sulfur recovery technology of S content less than 20% mainly contains direct oxidation method, LO-cat technique, and direct oxidation method technique adopts sour gas and air mixed, and be heated to temperature of reaction and enter reactor, under the effect of catalyzer, reaction formula is: H
2s+1/2O
2→ S+H
2o, direct oxidation method technique is applicable to process lower concentration sour gas, but catalyzer is to NH
3, CO, the impurity such as methyl alcohol is responsive, so this technique cannot process the more sour gas of impurity.
LO-cat technique is a kind of liquid phase oxidation technique processing lower concentration acid gas, and it adopts distinctive chelated iron catalyzer H
2s transforms into elemental sulfur.Overall process is: H
2s+1/2O
2→ H
2o+S, the oxygen in reaction is provided by the air blasting catalyst solution.Lo-Cat technique is to H
2s concentration level does not limit, but moisturely in sour gas can dilute chelated iron catalyst solution, and this technique cannot transform impurity such as the CO in sour gas, methyl alcohol in addition, so Lo-Cat technique also has limitation for the sour gas that process impurity is more.
Summary of the invention
The object of this invention is to provide a kind of recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas.
In order to achieve the above object, technical scheme of the present invention there is provided a kind of recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas, it is characterized in that, comprising: H Coal Chemical Industry process produced
2the volumetric concentration of S be 2% ~ 30% sour gas carry out Crouse's burning, the Process Gas that burning generates is carried out two-stage claus reaction, the tail gas that two-stage claus reaction produces is carried out hydrogenation-direct oxidation and wet scrubbing successively, reclaims the sulphur produced in Crouse's burning, two-stage claus reaction and hydrogenation-direct oxidation process.
Preferably, the step of described Crouse's burning comprises: burn spraying into burner for producing sulfur after the nitrogen atomization of molten sulfur by same temperature, simultaneously by H that Coal Chemical Industry process produces
2the volumetric concentration of S be 2% ~ 30%, the volumetric concentration of ammonia be 1% ~ 20% the H that produces of sour gas, combustion-supporting gas and Coal Chemical Industry process
2the volumetric concentration of S is 2% ~ 30%, do not contain the sour gas of ammonia respectively through containing propylhomoserin hot-air heater, enter burner for producing sulfur after remix after airheater and the preheating of clean sour gas well heater to burn, after the Process Gas produced in burner for producing sulfur enters waste heat boiler cooling, the major part of the Process Gas exporting out from waste heat boiler enters one-level condensate cooler and carries out condensing cooling, then enter two-stage claus reaction device and carry out two-stage claus reaction, remaining part is for heating the inlet gas of two-stage claus reaction device, the elemental sulfur produced in one-level condensate cooler enters sulphur sealed cans for reclaiming.
More preferably, described nitrogen is preheating to through steam heater or heating muff and is atomized with molten sulfur uniform temp again.
More preferably, as the H that Coal Chemical Industry process produces
2the volumetric concentration of S is 2% ~ 30%, when being not 200kcal/kg ~ 4000kcal/kg containing the calorific value of the sour gas of ammonia, described oxidizer is pure oxygen, oxygen enrichment or air.
More preferably, described burner for producing sulfur comprises prefix area, the H that described Coal Chemical Industry process produces
2the volumetric concentration of S be 2% ~ 30%, the volumetric concentration of ammonia be 1% ~ 20% sour gas first in prefix area, carry out preposition burning ammonia, form more than 1250 DEG C high-temperature zones, ammonia all decomposed.
More preferably, described oxidizer is preheating to more than 120 DEG C, the H that Coal Chemical Industry process produces
2the volumetric concentration of S be 2% ~ 30%, the volumetric concentration of ammonia be 1% ~ 20% sour gas be preheating to more than 120 DEG C, the H that Coal Chemical Industry process produces
2the volumetric concentration of S is 2% ~ 30%, is not preheating to after more than 130 DEG C containing the sour gas of ammonia, the H that the Coal Chemical Industry process after a part and preheating produces
2the volumetric concentration of S be 2% ~ 30%, the volumetric concentration of ammonia be 1% ~ 20% sour gas be mixed into burner for producing sulfur and burn, rest part is diverted to burner for producing sulfur combustion flame envelope front end, by regulating two-part bypass flow, regulate the burner hearth front and back end temperature of burner for producing sulfur.
Preferably, the step of described two-stage claus reaction comprises: the Process Gas produced that Crouse burnt carries out claus reaction in two-stage claus reaction device, the Process Gas that reaction produces is after condensing cooling, the elemental sulfur produced enters sulphur sealed cans for reclaiming, and the tail gas produced carries out hydrogenation-direct oxidation and wet scrubbing successively.
Preferably, the step of described hydrogenation-direct oxidation comprises: the tail gas that two-stage claus reaction produces first is heated to 200 DEG C ~ 250 DEG C by electric heater again through tail gas gas-to-gas heat exchanger, enter hydrogenator, pass into hydrogen in hydrogenator inter-sync and carry out hydrogenation reaction, from hydrogenator Process Gas out through the 4th water cooler, direct oxidation reactor is entered after being cooled to 150 ~ 180 DEG C, pass into air in the inter-sync of direct oxidation reactor and carry out oxidizing reaction, flow container is divided from entering hydrogenation tail gas after direct oxidation reactor Process Gas out enters the 5th condensate cooler, molten sulfur storage tank is entered for reclaiming after the elemental sulfur generated is separated with Process Gas, Process Gas goes out hydrogenation tail gas and divides flow container laggard row wet scrubbing.
Preferably, the step of described wet scrubbing comprises: divide flow container Process Gas Process Gas out to absorb H via after surge tank by high energy Venturi tube and the abundant hybrid reaction of circulation alkali liquor pumped into from washing tower from hydrogenation tail gas
2s and SO
2, then after the purification of washing tower filler separatory, discharging directly into atmosphere.
Compared with prior art, the invention has the beneficial effects as follows:
The present invention is a kind of for low heat value, the less energy-consumption of polymictic Acidic Gas Treating, the recovery technology of sulfur of high exhaust gas purification rate: comprise molten sulfur circulation, nitrogen atomization, preposition burning ammonia, subregion burning combination process, and secondary claus reaction, middle temperature blending, the direct oxidation of Claus tail-gas hydrogenation reduction-air, wet scrubbing etc., ensure the burning sulphur temperature of low heat value raw material sour gas, decompose detrimental impurity in raw material sour gas simultaneously, the Process Gas that burning generates enters second step two-stage claus reaction part, sulfur recovery rate reaches more than 99.7%, air is arranged after cleaning of off-gas, SO in tail gas
2concentration is lower than 50mg/Nm
3-dry, washing part externally discharged waste water meets in line standard.
Accompanying drawing explanation
Fig. 1 is Crouse's burning, two-stage claus reaction some processes schema;
Fig. 2 is tail gas hydrogenation-direct oxidation some processes schema;
Fig. 3 is tail gas wet method washing some processes schema.
Embodiment
Below in conjunction with specific embodiment, set forth the present invention further.Should be understood that these embodiments are only not used in for illustration of the present invention to limit the scope of the invention.In addition should be understood that those skilled in the art can make various changes or modifications the present invention, and these equivalent form of values fall within the application's appended claims limited range equally after the content of having read the present invention's instruction.
Embodiment
A recovery technology of sulfur for molten sulfur circular treatment lower concentration sour gas, by the H that Coal Chemical Industry process produces
2the volumetric concentration of S is the sour gas of 5% and the H of Coal Chemical Industry process generation
2the volumetric concentration of S be 15%, the volumetric concentration of ammonia be 18% sour gas carry out Crouse's burning, the Process Gas that burning generates is carried out two-stage claus reaction, the tail gas that two-stage claus reaction produces is carried out hydrogenation-direct oxidation and wet scrubbing successively, reclaim the sulphur produced in Crouse's burning, two-stage claus reaction and hydrogenation-direct oxidation process, specific as follows:
The first step: Crouse burn: with the Crouse of routine burn unlike: molten sulfur is delivered to reaction of Salmon-Saxl burner entrance processed from molten sulfur pond by liquid sulfur pump, with the nitrogen of equal temperature, molten sulfur is atomized, oxidizer can select pure oxygen, oxygen enrichment or air, and be preheating to more than 120 DEG C, after above-mentioned material enters burner combustion, molten sulfur is all converted into SO
2, this measure is used for supplementing acid gas firing heat; All the other sour gas combustion parts are identical with conventional Crouse's burning process.
As shown in Figure 1, the nitrogen from device general facilities being preheating to 120 DEG C through steam heater, burning spraying into burner for producing sulfur 4 after the nitrogen atomization of the molten sulfur of 120 DEG C by same temperature, simultaneously by H that Coal Chemical Industry process produces
2the volumetric concentration of S be 15%, H that the volumetric concentration of ammonia is 18%, calorific value is 1500kcal/kg sour gas, combustion-supporting gas and Coal Chemical Industry process produce
2the volumetric concentration of S is 5%, containing ammonia, to be 400kcal/kg sour gas burn respectively through entering burner for producing sulfur 4 after mixing according to volume ratio 4: 3 after being preheating to 130 DEG C containing propylhomoserin hot-air heater 1, airheater 2 and clean sour gas well heater 3 calorific value again, in burner for producing sulfur 4, containing H
2s is completely broken down containing the ammonia, hydro carbons etc. in ammonia acid waste gas, part H
2s is converted into SO
2, the SO of generation
2continue and remaining H
2s generates elemental sulfur by high temperature claus reaction, and what burner for producing sulfur 4 produced contains elemental sulfur, H
2s, SO
2enter waste heat boiler 5 etc. the Process Gas of component and be cooled to 800 DEG C, waste heat boiler 5 produces 4.0Mpa steam simultaneously, the major part of the Process Gas exporting out from waste heat boiler 5 enters one-level condensate cooler 6 and carries out condensing cooling, then enter two-stage claus reaction device 7 and carry out two-stage claus reaction, remaining part is for heating the inlet gas of two-stage claus reaction device 7, and the elemental sulfur produced in one-level condensate cooler 6 enters sulphur sealed cans 8 for reclaiming.
Described burner for producing sulfur 4 comprises prefix area, the H that described Coal Chemical Industry process produces
2the volumetric concentration of S be 15%, the volumetric concentration of ammonia be 18% sour gas first in prefix area, carry out preposition burning ammonia, form more than 1250 DEG C high-temperature zones, ammonia all decomposed.The H that Coal Chemical Industry process produces
2the volumetric concentration of S is 5%, not containing after the sour gas preheating of ammonia, the H that the Coal Chemical Industry process after a part and preheating produces
2the volumetric concentration of S be 15%, the volumetric concentration of ammonia be 18% the sour gas prefix area that is mixed into burner for producing sulfur 4 burn, rest part is diverted to burner for producing sulfur 4 combustion flame envelope front end, by regulating two-part bypass flow, regulate the burner hearth front and back end temperature of burner for producing sulfur 4.
Second step: two-stage claus reaction: major part enters one-level condensate cooler 6 from the Process Gas of waste heat boiler outlet from waste heat boiler 5 outlet and is cooled to 160 DEG C carries out conventional Claus reaction two-stage claus reaction device 7, conveniently two-stage claus reaction flow process, adopt warm fusion technique in two-stage, through 2 claus reaction devices, according to SO
2+ 2H
2s=3S+2H
2o reacts, and generates elemental sulfur.Rest part Process Gas is divided into two strands from waste heat boiler 5 outlet, through mixing valve heating two-stage claus reaction device 7 inlet gas.
Be separated with Process Gas after the elemental sulfur generated in burner for producing sulfur 4 is condensed and cools and enter via entering molten sulfur storage tank after sulphur sealed cans 8 for reclaiming.Process Gas after elemental sulfur is separated is through two-stage claus reaction device 7 and B-grade condensation water cooler 9, pass through claus reaction, generate elemental sulfur, B-grade condensation water cooler 9 Process Gas out enters three grades of condensate coolers, 10, three grades of condensate coolers 10 tail gas out again and enters follow-up hydrogenation-direct oxidation process.
3rd step: hydrogenation-direct oxidation: as shown in Figure 2, first 220 DEG C are heated to by electric heater 12 again through tail gas gas-to-gas heat exchanger 11 from three grades of condensate cooler 10 top tail gas out, enter hydrogenator 13, pass into hydrogen in hydrogenator 13 inter-sync, according to following reaction SO
2+ 3H
2=H
2s+2H
2o, SO in tail gas
2be reduced to H
2s.From hydrogenator 13 Process Gas out through the 4th water cooler 14, enter direct oxidation reactor 15 after being cooled to 150 DEG C, pass into air in direct oxidation reactor 15 inter-sync, pass through H
2s+1/2O
2=S+H
2o reacts, more than 95% H
2s generates elemental sulfur, all the other a small amount of H
2s passes through H
2s+3/2O
2=SO
2+ H
2o reaction generates SO
2.Flow container 17 is divided from entering hydrogenation tail gas after direct oxidation reactor 15 Process Gas out enters the 5th condensate cooler 16, enter molten sulfur storage tank after the elemental sulfur generated is separated with Process Gas for reclaiming, Process Gas goes out after hydrogenation tail gas divides flow container 17 to enter wet scrubbing part.
4th step: as shown in Figure 3, divides the H of flow container 17 Process Gas out only containing trace from hydrogenation tail gas
2s and SO
2, enter wet scrubbing part.Process Gas is fully mixed with the circulation alkali liquor pumped into from washing tower 20 by high energy Venturi tube 19 via after surge tank 18, by the H in Process Gas
2s and SO
2absorb in liquid phase, SO occurs simultaneously
2+ 2NaOH=Na
2sO
3+ H
2o, 2HS
-+ SO
3 2-+ 4H
+=3H
2the reactions such as O+3S.H
2s and SO
2process Gas after absorption is again after the purification of washing tower 20 filler separatory, and discharging directly into atmosphere, enters SO in the gas of air
2emission concentration be less than 50mg/m
3.H is absorbed in high energy Venturi tube 19
2s and SO
2after alkali lye flow automatically back bottom washing tower 20 and reuse as circulation alkali liquor.Major part circulation alkali liquor returns high energy Venturi tube 19 through recycle pump 21, and remainder circulation alkali liquor loops back jet aeration device at the bottom of washing tower 20 tower, and Na occurs the air mixed come with blower fan
2sO
3+ 1/2O
2=Na
2sO
4reaction, reduces the COD of circulation alkali liquor, makes to meet in line standard through filter 22 outer row brackish water.Washing tower 20 supplements alkali lye and fresh water in good time.
Claims (9)
1. a recovery technology of sulfur for molten sulfur circular treatment lower concentration sour gas, is characterized in that, comprising: H Coal Chemical Industry process produced
2the volumetric concentration of S be 2% ~ 30% sour gas carry out Crouse's burning, the Process Gas that burning generates is carried out two-stage claus reaction, the tail gas that two-stage claus reaction produces is carried out hydrogenation-direct oxidation and wet scrubbing successively, reclaims the sulphur produced in Crouse's burning, two-stage claus reaction and hydrogenation-direct oxidation process.
2. the recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas as claimed in claim 1, it is characterized in that, the step of described Crouse's burning comprises: burn spraying into burner for producing sulfur (4) after the nitrogen atomization of molten sulfur by same temperature, simultaneously by H that Coal Chemical Industry process produces
2the volumetric concentration of S be 2% ~ 30%, the volumetric concentration of ammonia be 1% ~ 20% the H that produces of sour gas, combustion-supporting gas and Coal Chemical Industry process
2the volumetric concentration of S is 2% ~ 30%, do not contain the sour gas of ammonia respectively through containing propylhomoserin hot-air heater (1), enter burner for producing sulfur (4) after remix after airheater (2) and clean sour gas well heater (3) preheating to burn, after the Process Gas produced in burner for producing sulfur (4) enters waste heat boiler (5) cooling, enter one-level condensate cooler (6) from the major part of waste heat boiler (5) outlet Process Gas out and carry out condensing cooling, then enter two-stage claus reaction device (7) and carry out two-stage claus reaction, remaining part is for heating the inlet gas of two-stage claus reaction device (7), the elemental sulfur produced in one-level condensate cooler (6) enters sulphur sealed cans (8) for reclaiming.
3. the recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas as claimed in claim 2, it is characterized in that, described nitrogen is preheating to through steam heater or heating muff and is atomized with molten sulfur uniform temp again.
4. the recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas as claimed in claim 2, is characterized in that, as the H that Coal Chemical Industry process produces
2the volumetric concentration of S is 2% ~ 30%, when being not 200kcal/kg ~ 4000kcal/kg containing the calorific value of the sour gas of ammonia, described oxidizer is pure oxygen, oxygen enrichment or air.
5. the recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas as claimed in claim 2, it is characterized in that, described burner for producing sulfur (4) comprises prefix area, the H that described Coal Chemical Industry process produces
2the volumetric concentration of S be 2% ~ 30%, the volumetric concentration of ammonia be 1% ~ 20% sour gas first in prefix area, carry out preposition burning ammonia, form more than 1250 DEG C high-temperature zones, ammonia all decomposed.
6. the recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas as claimed in claim 2, it is characterized in that, described oxidizer is preheating to more than 120 DEG C, the H that Coal Chemical Industry process produces
2the volumetric concentration of S be 2% ~ 30%, the volumetric concentration of ammonia be 1% ~ 20% sour gas be preheating to more than 120 DEG C, the H that Coal Chemical Industry process produces
2the volumetric concentration of S is 2% ~ 30%, is not preheating to after more than 130 DEG C containing the sour gas of ammonia, the H that the Coal Chemical Industry process after a part and preheating produces
2the volumetric concentration of S be 2% ~ 30%, the volumetric concentration of ammonia be 1% ~ 20% sour gas be mixed into burner for producing sulfur (4) and burn, rest part is diverted to burner for producing sulfur (4) combustion flame envelope front end, by regulating two-part bypass flow, regulate the burner hearth front and back end temperature of burner for producing sulfur (4).
7. the recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas as claimed in claim 1, it is characterized in that, the step of described two-stage claus reaction comprises: the Process Gas produced that Crouse burnt carries out claus reaction in two-stage claus reaction device (7), the Process Gas that reaction produces is after condensing cooling, the elemental sulfur produced enters sulphur sealed cans (8) for reclaiming, and the tail gas produced carries out hydrogenation-direct oxidation and wet scrubbing successively.
8. the recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas as claimed in claim 1, it is characterized in that, the step of described hydrogenation-direct oxidation comprises: the tail gas that two-stage claus reaction produces first is heated to 200 DEG C ~ 250 DEG C by electric heater (12) again through tail gas gas-to-gas heat exchanger (11), enter hydrogenator (13), pass into hydrogen in hydrogenator (13) inter-sync and carry out hydrogenation reaction, from hydrogenator (13) Process Gas out through the 4th water cooler (14), direct oxidation reactor (15) is entered after being cooled to 150 ~ 180 DEG C, pass into air in direct oxidation reactor (15) inter-sync and carry out oxidizing reaction, flow container (17) is divided from entering hydrogenation tail gas after direct oxidation reactor (15) Process Gas out enters the 5th condensate cooler (16), after the elemental sulfur generated is separated with Process Gas, enter molten sulfur storage tank for reclaiming, Process Gas goes out after hydrogenation tail gas divides flow container (17) to carry out wet scrubbing.
9. the recovery technology of sulfur of molten sulfur circular treatment lower concentration sour gas as claimed in claim 1, it is characterized in that, the step of described wet scrubbing comprises: divide flow container (17) Process Gas out to absorb H by high energy Venturi tube (19) and the abundant hybrid reaction of circulation alkali liquor pumped into from washing tower (20) afterwards via surge tank (18) from hydrogenation tail gas
2s and SO
2, then after the purification of washing tower (20) filler separatory, discharging directly into atmosphere.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410788412.6A CN104528659B (en) | 2014-12-17 | 2014-12-17 | Sulfur recycling process for circularly treating low-concentration acidy gas by utilizing liquid sulfur |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410788412.6A CN104528659B (en) | 2014-12-17 | 2014-12-17 | Sulfur recycling process for circularly treating low-concentration acidy gas by utilizing liquid sulfur |
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| Publication Number | Publication Date |
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| CN104528659A true CN104528659A (en) | 2015-04-22 |
| CN104528659B CN104528659B (en) | 2017-04-12 |
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| US11224838B2 (en) | 2019-12-26 | 2022-01-18 | Jiangnan Environmental Protection Group Inc. | Controlling aerosol production during absorption in ammonia-based desulfurization |
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| US9370745B2 (en) | 2013-04-24 | 2016-06-21 | Jiangsu New Century Jiangnan Environmental Protection Co., Ltd | Flue gas-treating method and apparatus for treating acidic tail gas by using ammonia process |
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| US10406477B2 (en) | 2017-03-15 | 2019-09-10 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
| US10413864B2 (en) | 2017-03-15 | 2019-09-17 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
| US10561982B2 (en) | 2017-05-25 | 2020-02-18 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desulfurization process and apparatus |
| US10471383B2 (en) | 2017-05-25 | 2019-11-12 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10343110B2 (en) | 2017-05-25 | 2019-07-09 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10413865B2 (en) | 2017-05-25 | 2019-09-17 | Jiangnan Enviromental Protection Group Inc. | Ammonia-based desulfurization process and apparatus |
| US10406478B2 (en) | 2017-05-25 | 2019-09-10 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desulfurization process and apparatus |
| US10399033B2 (en) | 2017-05-25 | 2019-09-03 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desulfurization process and apparatus |
| US10583386B2 (en) | 2017-06-14 | 2020-03-10 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US10589212B2 (en) | 2017-06-14 | 2020-03-17 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US10618001B2 (en) | 2017-07-03 | 2020-04-14 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10556205B2 (en) | 2017-07-03 | 2020-02-11 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10561984B2 (en) | 2017-07-03 | 2020-02-18 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10427097B2 (en) | 2017-07-03 | 2019-10-01 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10421040B2 (en) | 2017-07-03 | 2019-09-24 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10357741B2 (en) | 2017-09-07 | 2019-07-23 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
| US10449488B2 (en) | 2017-09-07 | 2019-10-22 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
| US10369517B2 (en) | 2017-09-07 | 2019-08-06 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
| US11027234B2 (en) | 2018-04-13 | 2021-06-08 | Jiangnan Environmental Protection Group Inc. | Oxidization of ammonia desulfurization solution |
| US10953365B2 (en) | 2018-07-20 | 2021-03-23 | Jiangnan Environmental Protection Group Inc. | Acid gas treatment |
| US11529584B2 (en) | 2018-07-20 | 2022-12-20 | Jiangnan Environmental Protection Group Inc. | Acid gas treatment |
| CN112337280A (en) * | 2019-08-09 | 2021-02-09 | 中国石化工程建设有限公司 | Claus flow-dividing sulfur recovery system and process |
| US11224838B2 (en) | 2019-12-26 | 2022-01-18 | Jiangnan Environmental Protection Group Inc. | Controlling aerosol production during absorption in ammonia-based desulfurization |
| CN113264508A (en) * | 2020-02-17 | 2021-08-17 | 中国石油天然气集团有限公司 | Sulfur recovery method and device |
| CN113264508B (en) * | 2020-02-17 | 2022-08-05 | 中国石油天然气集团有限公司 | Sulfur recovery method and device |
| CN115304034A (en) * | 2022-08-02 | 2022-11-08 | 新乡中新化工有限责任公司 | Application system and method of nitrogen pipeline of Claus sulfur recovery device |
| CN115304034B (en) * | 2022-08-02 | 2024-01-26 | 新乡中新化工有限责任公司 | Application system and method of nitrogen pipeline of Claus sulfur recovery device |
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Effective date of registration: 20190220 Address after: 116000 No. 123, Datong Street, Xigang District, Dalian City, Liaoning Province, Unit 11, Floor 6 Patentee after: Dalian Hannuo Engineering Technology Co., Ltd. Address before: 116000 No. 34 Tangshan Street, Xigang District, Dalian City, Liaoning Province Patentee before: Tian Xiaoliang |