CN104528659B - 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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- CN104528659B CN104528659B CN201410788412.6A CN201410788412A CN104528659B CN 104528659 B CN104528659 B CN 104528659B CN 201410788412 A CN201410788412 A CN 201410788412A CN 104528659 B CN104528659 B CN 104528659B
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- sour gas
- ammonia
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 103
- 238000000034 method Methods 0.000 title claims abstract description 90
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 85
- 239000011593 sulfur Substances 0.000 title claims abstract description 85
- 239000007788 liquid Substances 0.000 title claims abstract description 10
- 238000004064 recycling Methods 0.000 title abstract description 6
- 238000006243 chemical reaction Methods 0.000 claims abstract description 45
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 29
- 230000003647 oxidation Effects 0.000 claims abstract description 25
- 239000003245 coal Substances 0.000 claims abstract description 24
- 238000002485 combustion reaction Methods 0.000 claims abstract description 8
- 238000001311 chemical methods and process Methods 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 82
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 67
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 64
- 229910021529 ammonia Inorganic materials 0.000 claims description 31
- 239000000126 substance Substances 0.000 claims description 21
- 238000011084 recovery Methods 0.000 claims description 19
- 238000005984 hydrogenation reaction Methods 0.000 claims description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 16
- 238000005516 engineering process Methods 0.000 claims description 16
- 238000005200 wet scrubbing Methods 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 10
- 239000003513 alkali Substances 0.000 claims description 9
- 239000002918 waste heat Substances 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 238000005201 scrubbing Methods 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 238000000889 atomisation Methods 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 4
- 239000005864 Sulphur Substances 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims description 2
- 239000000945 filler Substances 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims 1
- 239000012535 impurity Substances 0.000 abstract description 6
- 239000002994 raw material Substances 0.000 abstract description 4
- 238000002156 mixing Methods 0.000 abstract description 3
- 238000005406 washing Methods 0.000 abstract description 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 239000002253 acid Substances 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 239000007800 oxidant agent Substances 0.000 description 3
- 230000002378 acidificating effect Effects 0.000 description 2
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- DWNBOPVKNPVNQG-LURJTMIESA-N (2s)-4-hydroxy-2-(propylamino)butanoic acid Chemical compound CCCN[C@H](C(O)=O)CCO DWNBOPVKNPVNQG-LURJTMIESA-N 0.000 description 1
- 239000007832 Na2SO4 Substances 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 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
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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 low concentration sour gas, for sulfur recovery facility
Design, belongs to sulphur recovery field.
Background technology
For the various low concentration Acidic Gas Treatings that Coal Chemical Industry process is produced, generally containing H2S concentration is low, such as low temperature first
The sour gas that Chun Xi workshop sections come contains CO2Height, H2S concentration 25% or so, and containing a small amount of methanol, and the acid that phenol recovery ammonia workshop section comes
Property gas contain NH3, containing H2O, H2S concentration 4% or so, due to the calorific value of these sour gas it is very low, even allocate pure oxygen into also cannot reach
To ammonia temperature is burnt, the claus process of shunting also cannot be processed.
H is processed at present2Sulfur recovery technology of the S contents below 20% mainly has direct oxidation method, LO-cat techniques, direct oxygen
Change method technique is mixed using sour gas with air, is heated to reaction temperature and is entered reactor, in the presence of catalyst, reaction equation
For：H2S+1/2O2→S+H2O, direct oxidation method technique is applied to process low concentration sour gas, but catalyst is to NH3, CO, methanol
It is sensitive Deng impurity, so the technique cannot process the more sour gas of impurity.
LO-cat techniques are a kind of liquid phase oxidation techniques of process low concentration acid gas, and it adopts distinctive chelating iron catalyst
H2S transforms into elemental sulfur.Overall process is：H2S+1/2O2→H2O+S, the oxygen in reaction is by blasting catalyst solution
Air provide.Lo-Cat techniques are to H2S concentration levels are not limited, but in sour gas it is aqueous can dilute chelating iron catalyst it is molten
Liquid, in addition the technique cannot be converted to impurity such as the CO in sour gas, methanol, so Lo-Cat techniques are more for impurity is processed
Sour gas also have limitation.
The content of the invention
It is an object of the invention to provide a kind of recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas.
In order to achieve the above object, the technical scheme is that there is provided a kind of molten sulfur circular treatment low concentration sour gas
Recovery technology of sulfur, it is characterised in that include：The H that Coal Chemical Industry process is produced2The volumetric concentration of S is 2%～30% acid
Property gas carry out Crouse's burning, by burning generate Process Gas carry out two-stage claus reaction, by two-stage claus reaction produce
Tail gas carry out being hydrogenated with-direct oxidation and wet scrubbing successively, reclaim Crouse's burning, two-stage claus reaction and hydrogenation-straight
Connect the sulfur produced in oxidizing process.
Preferably, the step of described Crouse is burnt includes：System will be sprayed into after nitrogen atomization of the molten sulfur with same temperature
Sulphur burner is burnt, while the H that Coal Chemical Industry process is produced2The volumetric concentration of S is 2%～30%, ammonia volume
Concentration is the H that 1%～20% sour gas, combustion-supporting gas and Coal Chemical Industry process is produced2The volumetric concentration of S be 2%～30%, no
Sour gas containing ammonia is respectively through hot-air heater containing propylhomoserin, air heater and cleans after the preheating of sour gas heater again
Burnt into burner for producing sulfur after mixing, the Process Gas produced in burner for producing sulfur are entered after waste heat boiler cooling, from useless
The major part of hot pot outlet of still Process Gas out carries out condensation cooling into one-level condensate cooler, subsequently into two-stage gram labor
This reactor carries out two-stage claus reaction, and remaining part is used to heat the inlet gas of two-stage claus reaction device, one
The elemental sulfur produced in level condensate cooler enters sulfur sealed cans to be used to reclaim.
It is highly preferred that described nitrogen is preheating to through steam heater or heating muff mutually synthermal with molten sulfur carrying out again
Atomization.
It is highly preferred that as the H of Coal Chemical Industry process generation2The volumetric concentration of S is 2%～30%, sour gas without ammonia
Calorific value when being 200kcal/kg～4000kcal/kg, described oxidizer is pure oxygen, oxygen-enriched or air.
It is highly preferred that described burner for producing sulfur includes prefix area, the H that described Coal Chemical Industry process is produced2The volume of S is dense
Spend for 2%～30%, the sour gas that the volumetric concentration of ammonia is 1%～20% first preposition burning ammonia, shape are carried out in prefix area
Into 1250 DEG C of high temperature above areas, ammonia is set all to decompose.
It is highly preferred that described oxidizer is preheating to more than 120 DEG C, the H that Coal Chemical Industry process is produced2The volumetric concentration of S is
2%～30%, the sour gas that the volumetric concentration of ammonia is 1%～20% be preheating to more than 120 DEG C, what Coal Chemical Industry process was produced
H2The volumetric concentration of S is the coal after 2%～30%, sour gas without ammonia is preheating to more than 130 DEG C, after a part and preheating
The H that chemical process is produced2The volumetric concentration of S be 2%～30%, the sour gas that the volumetric concentration of ammonia is 1%～20% mixes
Conjunction is burnt into burner for producing sulfur, and remainder is diverted to burning flame envelope front end in burner for producing sulfur, by adjusting two
Point bypass flow adjusting the burner hearth front and back end temperature of burner for producing sulfur.
Preferably, the step of described two-stage claus reaction, includes：Crouse is burnt into the Process Gas for producing in two-stage
Claus reaction is carried out in claus reaction device, after reacting the condensed cooling of Process Gas for producing, produced elemental sulfur is entered
Sulfur sealed cans are used to reclaim, and produced tail gas carries out being hydrogenated with successively-direct oxidation and wet scrubbing.
Preferably, the step of described hydrogenation-direct oxidation includes：The tail gas that two-stage claus reaction is produced is first passed through
Tail gas gas-to-gas heat exchanger is heated to 200 DEG C～250 DEG C by electric heater again, into hydrogenation reactor, in hydrogenation reactor
Synchronously being passed through hydrogen carries out hydrogenation reaction, from the hydrogenation reactor coolers of Process Gas Jing the 4th out, is cooled to 150～180
Direct oxidation reactor is entered after DEG C, being synchronously passed through air in direct oxidation reactor carries out oxidation reaction, from direct oxidation
Reactor Process Gas out are entered after the 5th condensate cooler and enter hydrogenation tail gas point flow container, the elemental sulfur and Process Gas of generation
Molten sulfur storage tank is entered after separation to be used to reclaim, and Process Gas to go out to be hydrogenated with and carry out wet scrubbing after tail gas point flow container.
Preferably, the step of described wet scrubbing includes：From hydrogenation tail gas point flow container Process Gas Process Gas Jing out
Reactive absorption H is sufficiently mixed with the circulation alkali liquor pumped into from scrubbing tower by high energy Venturi tube by after surge tank2S and SO2, then
After scrubbed tower packing point liquid purification, discharging directly into atmosphere.
Compared with prior art, the invention has the beneficial effects as follows：
The present invention be it is a kind of for low heat value, the low energy consumption of polymictic Acidic Gas Treating, high exhaust gas purifying rate sulfur
Recovery process：Including molten sulfur circulation, nitrogen atomization, preposition burning ammonia, subregion burning group technology, and two grades of claus reactions,
Middle temperature blending, Claus tail-gas hydrogenation reduction-air direct oxidation, wet scrubbing etc., it is ensured that the combustion of low heat value raw material sour gas
Sulfur temperature is fired, while decomposing objectionable impurities in raw material sour gas, the Process Gas for generating that burn enter second step two-stage Crouse
Reactive moieties, sulfur recovery rate up to more than 99.7%, cleaning of off-gas heel row air, SO in tail gas2Concentration is less than 50mg/Nm3- dry,
Washing part externally discharged waste water meets in line standard.
Description of the drawings
Fig. 1 is Crouse's burning, two-stage claus reaction some processes flow chart；
Fig. 2 is tail gas hydrogenation-direct oxidation some processes flow chart；
Fig. 3 is that tail gas wet method washs some processes flow chart.
Specific embodiment
With reference to specific embodiment, the present invention is expanded on further.It should be understood that these embodiments are merely to illustrate the present invention
Rather than restriction the scope of the present invention.In addition, it is to be understood that after the content for having read instruction of the present invention, people in the art
Member can make various changes or modifications to the present invention, and these equivalent form of values equally fall within the application appended claims and limited
Scope.
Embodiment
A kind of recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas, the H that Coal Chemical Industry process is produced2The body of S
Product concentration is the H that 5% sour gas and Coal Chemical Industry process are produced2The volumetric concentration of S be 15%, the volumetric concentration of ammonia be
18% sour gas carries out Crouse's burning, the Process Gas that burning is generated is carried out into two-stage claus reaction, by two-stage Crouse
The tail gas that reaction is produced carries out being hydrogenated with successively-direct oxidation and wet scrubbing, reclaim Crouse's burning, two-stage claus reaction and
The sulfur produced during hydrogenation-direct oxidation, it is specific as follows：
The first step：Crouse is burnt：Unlike burning from conventional Crouse：Molten sulfur is defeated by liquid sulfur pump from molten sulfur pond
Reaction of Salmon-Saxl burner entrance processed is delivered to, is atomized molten sulfur with the nitrogen of same equitemperature, oxidizer can select pure oxygen, oxygen-enriched or sky
Gas, and it is preheating to more than 120 DEG C, above-mentioned material is entered after burner combustion, and molten sulfur is completely converted into SO2, this measure be used for mend
Fill sour gas calory burning；Remaining sour gas combustion parts is identical with Crouse's burning process of routine.
As shown in figure 1,120 DEG C will be preheating to from the nitrogen Jing steam heaters of device public work, by 120 DEG C of liquid
Sulfur is burnt with penetrating burner for producing sulfur 4 after the nitrogen atomization of same temperature, while the H that Coal Chemical Industry process is produced2The body of S
Product concentration be 15%, the volumetric concentration of ammonia be sour gas, combustion-supporting gas and coalification that 18%, calorific value is 1500kcal/kg
The H that work process is produced2The volumetric concentration of S is 5%, without ammonia, calorific value be 400kcal/kg sour gas respectively through containing ammonia
Acid hot-air heater 1, air heater 2 and cleaning sour gas heater 3 are mixed according still further to volume ratio 4: 3 after being preheating to 130 DEG C
Burnt into burner for producing sulfur 4 after conjunction, in burner for producing sulfur 4, containing H2Ammonia, hydro carbons in the acid waste gas containing ammonia of S
Etc. being completely broken down, part H2S is converted into SO2, the SO of generation2Continue and remaining H2S is generated single by high temperature claus reaction
Matter sulfur, burner for producing sulfur 4 produce containing elemental sulfur, H2S、SO2800 are cooled to etc. the Process Gas of component into waste heat boiler 5
DEG C, waste heat boiler 5 produces 4.0Mpa steam simultaneously, and the major part of the Process Gas for exporting out from waste heat boiler 5 is cold into one-level
Solidifying cooler 6 carries out condensation cooling, and subsequently into two-stage claus reaction device 7 two-stage claus reaction, remaining part are carried out
For heating the inlet gas of two-stage claus reaction device 7, the elemental sulfur produced in one-level condensate cooler 6 enters sulfur sealed cans
8 are used to reclaim.
Described burner for producing sulfur 4 includes prefix area, the H that described Coal Chemical Industry process is produced2The volumetric concentration of S is 15%
, the sour gas that the volumetric concentration of ammonia is 18% first preposition burning ammonia is carried out in prefix area, form 1250 DEG C of high temperature above areas,
Ammonia is set all to decompose.The H that Coal Chemical Industry process is produced2The volumetric concentration of S is 5%, after the preheating of the sour gas without ammonia, one
Divide the H produced with the Coal Chemical Industry process after preheating2The volumetric concentration of S be 15%, the acidity that the volumetric concentration of ammonia is 18%
Gas is mixed into the prefix area of burner for producing sulfur 4 and is burnt, and remainder is diverted in burner for producing sulfur 4 before burning flame envelope
End, by adjusting two-part bypass flow the burner hearth front and back end temperature of burner for producing sulfur 4 is adjusted.
Second step：Two-stage claus reaction：Most of Process Gas from waste heat boiler outlet from waste heat boiler 5 export into
Entering one-level condensate cooler 6 and being cooled to 160 DEG C carries out conventional Claus reaction in two-stage claus reaction device 7, according to normal
Rule two-stage claus reaction flow process, blends technique, through 2 claus reaction devices, according to SO using the middle temperature of two-stage2+2H2S=3S
+2H2O reacts, and generates elemental sulfur.Remainder Process Gas are divided into two strands from the outlet of waste heat boiler 5, and blended valve heats two-stage gram
The inlet gas of Louth reactor 7.
The elemental sulfur generated in burner for producing sulfur 4 is condensed after being segregated into via sulfur sealed cans 8 with Process Gas after cooling down
It is used to reclaim into molten sulfur storage tank.Process Gas after elemental sulfur is separated are cold through two-stage claus reaction device 7 and B-grade condensation
But device 9, by claus reaction, generate elemental sulfur, and the Process Gas out of B-grade condensation cooler 9 enter back into three-level condensation cooling
Device 10, the tail gas out of three-level condensate cooler 10 enters follow-up hydrogenation-direct oxidation and processes.
3rd step：Hydrogenation-direct oxidation：As shown in Fig. 2 the tail gas from the top of three-level condensate cooler 10 out is first passed through
Tail gas gas-to-gas heat exchanger 11 is heated to 220 DEG C by electric heater 12 again, into hydrogenation reactor 13, in hydrogenation reactor 13
Interior synchronization is passed through hydrogen, according to following reaction SO2+3H2=H2S+2H2O, SO in tail gas2It is reduced to H2S.From hydrogenation reactor
13 coolers 14 of Process Gas Jing the 4th out, enter direct oxidation reactor 15 after being cooled to 150 DEG C, in direct oxidation reaction
Air is synchronously passed through in device 15, by H2S+1/2O2=S+H2O reacts, more than 95% H2S generates elemental sulfur, remaining a small amount of H2S leads to
Cross H2S+3/2O2=SO2+H2O reactions generate SO2.The 5th condensation cooling is entered from the Process Gas out of direct oxidation reactor 15
Hydrogenation tail gas point flow container 17 is entered after device 16, the elemental sulfur of generation enters molten sulfur storage tank after separating with Process Gas be used to reclaim, mistake
Journey gas goes out to be hydrogenated with after tail gas point flow container 17 into wet scrubbing part.
4th step：As shown in figure 3, only containing micro H from the hydrogenation tail gas point Process Gas out of flow container 172S and SO2, enter
Enter wet scrubbing part.Process Gas via after surge tank 18 by high energy Venturi tube 19 and the circulation alkali that pumps into from scrubbing tower 20
Liquid is sufficiently mixed, by the H in Process Gas2S and SO2In absorbing liquid phase, while there is SO2+ 2NaOH=Na2SO3+H2O、2HS-+
SO3 2-+4H+=3H2O+3S etc. reacts.H2S and SO2Again the filler of scrubbed tower 20 divides after liquid purification Process Gas after absorption, in line
Air, enters SO in the gas of air2Concentration of emission be less than 50mg/m3.H is absorbed in high energy Venturi tube 192S and SO2Afterwards
Alkali liquor flows automatically go back to the bottom of scrubbing tower 20 as circulation alkali liquor recycling.Most of circulation alkali liquor Jing circulating pumps 21 return high energy text
Venturi 19, remainder circulation alkali liquor loops back the bottom of towe jet aeration device of scrubbing tower 20, and the air come with blower fan mixes, and occurs
Na2SO3+1/2O2=Na2SO4Reaction, reduces the COD of circulation alkali liquor, makes to meet in line mark via the outer row's brackish water of filter 22
It is accurate.Scrubbing tower 20 supplements alkali liquor and fresh water in good time.
Claims (8)
1. a kind of recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas, it is characterised in that include：By Coal Chemical Industry process
The H of generation2The volumetric concentration of S is that 2%～30% sour gas carries out Crouse's burning, and the Process Gas that burning is generated are carried out into two-stage
Claus reaction, the tail gas that two-stage claus reaction is produced is carried out being hydrogenated with successively-direct oxidation and wet scrubbing, reclaims gram labor
The sulfur produced during this burning, two-stage claus reaction and hydrogenation-direct oxidation；The step of described Crouse is burnt is wrapped
Include：Burner for producing sulfur will be sprayed into after nitrogen atomization of the molten sulfur with same temperature（4）Burnt, while Coal Chemical Industry process is produced
H2The volumetric concentration of S be 2%～30%, sour gas, combustion-supporting gas and the Coal Chemical Industry mistake that the volumetric concentration of ammonia is 1%～20%
The H that journey is produced2The volumetric concentration of S is 2%～30%, sour gas without ammonia respectively through hot-air heater containing propylhomoserin（1）, it is empty
Hot-air heater（2）And cleaning sour gas heater（3）Burner for producing sulfur is entered after remixing after preheating（4）Burnt, made
Sulphur burner（4）The Process Gas of middle generation enter waste heat boiler（5）After cooling, from waste heat boiler（5）Outlet Process Gas out
Major part enter one-level condensate cooler（6）Condensation cooling is carried out, subsequently into two-stage claus reaction device（7）Carry out two-stage
Claus reaction, remaining part is used to heat two-stage claus reaction device（7）Inlet gas, in one-level condensate cooler
（6）The elemental sulfur of middle generation enters sulfur sealed cans（8）For reclaiming.
2. the recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas as claimed in claim 1, it is characterised in that described
Nitrogen be preheating to through steam heater or heating muff and mutually synthermal with molten sulfur be atomized again.
3. the recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas as claimed in claim 1, it is characterised in that work as coal
The H that chemical process is produced2The volumetric concentration of S be 2%～30%, sour gas without ammonia calorific value be 200kcal/kg～
During 4000kcal/kg, described combustion-supporting gas is pure oxygen, oxygen-enriched or air.
4. the recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas as claimed in claim 1, it is characterised in that described
Burner for producing sulfur（4）Comprising prefix area, the H that described Coal Chemical Industry process is produced2The volumetric concentration of S be 2%～30%, ammonia
Volumetric concentration be that 1%～20% sour gas first carries out preposition burning ammonia in prefix area, form 1250 DEG C of high temperature above areas, make ammonia
Gas all decomposes.
5. the recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas as claimed in claim 1, it is characterised in that described
Combustion-supporting gas be preheating to more than 120 DEG C, the H that Coal Chemical Industry process is produced2The volumetric concentration of S is 2%～30%, ammonia volume
Concentration is that 1%～20% sour gas is preheating to more than 120 DEG C, the H that Coal Chemical Industry process is produced2The volumetric concentration of S be 2%～30%,
After sour gas without ammonia is preheating to more than 130 DEG C, the H that the Coal Chemical Industry process after a part and preheating is produced2The volume of S is dense
Spend for 2%～30%, the sour gas that the volumetric concentration of ammonia is 1%～20% be mixed into burner for producing sulfur（4）Burnt, its
It is remaining to be diverted partially to burner for producing sulfur（4）Interior burning flame envelope front end, sulfur combustion processed is adjusted by adjusting two-part bypass flow
Burn stove（4）Burner hearth front and back end temperature.
6. the recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas as claimed in claim 1, it is characterised in that described
Two-stage claus reaction the step of include：Crouse is burnt into the Process Gas for producing in two-stage claus reaction device（7）In enter
Row claus reaction, after reacting the condensed cooling of Process Gas for producing, produced elemental sulfur enters sulfur sealed cans（8）For returning
To receive, produced tail gas carries out being hydrogenated with successively-direct oxidation and wet scrubbing.
7. the recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas as claimed in claim 1, it is characterised in that described
Hydrogenation-direct oxidation the step of include：The tail gas that two-stage claus reaction is produced is first passed through into tail gas gas-to-gas heat exchanger（11）
Again by electric heater（12）200 DEG C～250 DEG C are heated to, into hydrogenation reactor（13）, in hydrogenation reactor（13）It is interior same
Step is passed through hydrogen carries out hydrogenation reaction, from hydrogenation reactor（13）The coolers of Process Gas Jing the 4th out（14）, it is cooled to 150
Direct oxidation reactor is entered after～180 DEG C（15）, in direct oxidation reactor（15）Interior synchronization is passed through air and carries out aoxidizing instead
Should, from direct oxidation reactor（15）Process Gas out enter the 5th condensate cooler（16）Hydrogenation tail gas point flow container is entered afterwards
（17）, after the elemental sulfur of generation is separated with Process Gas, it is used to reclaim into molten sulfur storage tank, Process Gas go out to be hydrogenated with tail gas point flow container
（17）After carry out wet scrubbing.
8. the recovery technology of sulfur of molten sulfur circular treatment low concentration sour gas as claimed in claim 1, it is characterised in that described
Wet scrubbing the step of include：From hydrogenation tail gas point flow container（17）Process Gas out are via surge tank（18）Pass through high energy afterwards
Venturi tube（19）With from scrubbing tower（20）The circulation alkali liquor for pumping into is sufficiently mixed reactive absorption H2S and SO2, then scrubbed tower
（20）After filler point liquid purification, discharging directly into atmosphere.
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