CN110329995A - Selective oxidation sulfur recovery facility and recovery process - Google Patents
Selective oxidation sulfur recovery facility and recovery process Download PDFInfo
- Publication number
- CN110329995A CN110329995A CN201910735975.1A CN201910735975A CN110329995A CN 110329995 A CN110329995 A CN 110329995A CN 201910735975 A CN201910735975 A CN 201910735975A CN 110329995 A CN110329995 A CN 110329995A
- Authority
- CN
- China
- Prior art keywords
- outlet
- reactor
- sulphur
- gas
- selective oxidation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 158
- 238000011084 recovery Methods 0.000 title claims abstract description 66
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 55
- 239000011593 sulfur Substances 0.000 title claims abstract description 55
- 230000003647 oxidation Effects 0.000 title claims abstract description 50
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 50
- 239000007789 gas Substances 0.000 claims abstract description 111
- 239000005864 Sulphur Substances 0.000 claims abstract description 102
- 238000009833 condensation Methods 0.000 claims abstract description 51
- 230000005494 condensation Effects 0.000 claims abstract description 50
- 230000008676 import Effects 0.000 claims abstract description 49
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 32
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 31
- 238000002156 mixing Methods 0.000 claims abstract description 27
- 238000010438 heat treatment Methods 0.000 claims abstract description 24
- 239000002918 waste heat Substances 0.000 claims abstract description 24
- 239000008246 gaseous mixture Substances 0.000 claims abstract description 18
- 238000001816 cooling Methods 0.000 claims abstract description 15
- 230000004044 response Effects 0.000 claims description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 15
- 229910052760 oxygen Inorganic materials 0.000 claims description 15
- 239000001301 oxygen Substances 0.000 claims description 15
- 239000003054 catalyst Substances 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 238000006555 catalytic reaction Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 2
- 239000001257 hydrogen Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 14
- 230000008569 process Effects 0.000 abstract description 8
- 239000000126 substance Substances 0.000 abstract description 4
- 239000003245 coal Substances 0.000 abstract description 3
- 229910001882 dioxygen Inorganic materials 0.000 description 8
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 238000006477 desulfuration reaction Methods 0.000 description 6
- 239000012495 reaction gas Substances 0.000 description 6
- 230000023556 desulfurization Effects 0.000 description 4
- 230000004520 agglutination Effects 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- YZCKVEUIGOORGS-IGMARMGPSA-N Protium Chemical compound [1H] YZCKVEUIGOORGS-IGMARMGPSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000012958 reprocessing Methods 0.000 description 2
- 238000009279 wet oxidation reaction Methods 0.000 description 2
- RBORURQQJIQWBS-QVRNUERCSA-N (4ar,6r,7r,7as)-6-(6-amino-8-bromopurin-9-yl)-2-hydroxy-2-sulfanylidene-4a,6,7,7a-tetrahydro-4h-furo[3,2-d][1,3,2]dioxaphosphinin-7-ol Chemical compound C([C@H]1O2)OP(O)(=S)O[C@H]1[C@@H](O)[C@@H]2N1C(N=CN=C2N)=C2N=C1Br RBORURQQJIQWBS-QVRNUERCSA-N 0.000 description 1
- 206010019233 Headaches Diseases 0.000 description 1
- XAQHXGSHRMHVMU-UHFFFAOYSA-N [S].[S] Chemical compound [S].[S] XAQHXGSHRMHVMU-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 231100000869 headache Toxicity 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000000622 irritating effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 210000002345 respiratory system Anatomy 0.000 description 1
- 231100000004 severe toxicity Toxicity 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 238000004073 vulcanization Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000003643 water by type 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
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
- C01B17/0426—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the catalytic conversion
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention belongs to technical field of coal chemical industry, it is related to a kind of selective oxidation sulfur recovery facility and recovery process, including gaseous mixture unit, first-stage reactor, waste heat boiler, condensation collection sulphur device, second reactor and cooling recovery unit；Gaseous mixture unit includes sequentially connected knockout drum, blower, heating tank and blending tank；The cooling recovery unit includes sequentially connected condenser and catches sulphur device；The tube side of tube side and waste heat boiler of the outlet of gaseous mixture unit through first-stage reactor is finally connected with the import of condensation collection sulphur device；The outlet of condensation collection sulphur device is connected with the heating tank import of gaseous mixture unit and the import of second reactor respectively；The outlet of the second reactor successively with condenser and catch sulphur device and be connected.Present invention process simple device is few, and investment is small, and operating cost is low, the rate of recovery is high, can be recycled the hydrogen sulfide gas of various concentration.
Description
Technical field
The invention belongs to technical field of coal chemical industry, it is related to a kind of sulfur recovery facility and technique, in particular to a kind of selection
Aoxidize sulfur recovery facility and recovery process.
Background technique
Hydrogen sulfide gas can be generated in chemical industry, especially coal chemical industry production, due to hydrogen sulfide gas severe toxicity, even if
Dilute hydrogen sulfide causes to have a headache also to respiratory tract and the irritating effect of eyes, when concentration reaches 1mg/L or higher, has to life
Danger will carry out purified treatment to hydrogen sulfide gas, can discharge after reaching discharge standard.And as the standard of environmental protection is wanted
Ask increasingly strict, in order to make the discharge of sulphur reach higher discharge standard, the requirement to hydrogen sulfide recovery processing technique is also higher.
At present since oxidizing process has treating capacity big, can continuous production the advantages of, in the industry using more.Oxidizing process
It is divided into dry oxidation and wet oxidation；Wet oxidation is to absorb catalysis oxidation in the solution, complex process and introducing solution, energy consumption
Greatly, not environmentally, product sulphur impurity is more, and sulfur speciation is bad；Dry oxidation makes oxidizing hydrogen sulfide gas at elemental sulfur under normal conditions
Or sulfur oxide, have the characteristics that treating capacity is big and continuous production, typical dry oxidation have Claus method and selective oxygen
The process of change method, claus process is complex, and equipment investment is high, and operating cost is high；And selective oxidation processes are simple, fit
Close the hydrogen sulfide containing gas for handling various concentration.
Summary of the invention
Based on the above background the problem of technology, it is few that the present invention provides a kind of simple process equipment, invests small, operation
It is at low cost, the rate of recovery is high, can be recycled various concentration hydrogen sulfide gas selective oxidation sulfur recovery facility and recycling work
Skill.
To achieve the goals above, the technical scheme adopted by the invention is as follows:
A kind of selective oxidation sulfur recovery facility, which is characterized in that the selective oxidation sulfur recovery facility includes mixing
Gas unit, first-stage reactor, waste heat boiler, condensation collection sulphur device, second reactor and cooling recovery unit；The gaseous mixture list
The tube side of tube side and waste heat boiler of the outlet through first-stage reactor of member is finally connected with the import of condensation collection sulphur device；It is described cold
The outlet of agglutination sulphur device is connected with the import of gaseous mixture unit and the import of second reactor respectively；The second reactor
Outlet is connected with cooling recovery unit；
The gaseous mixture unit includes sequentially connected knockout drum, blower, heating tank and blending tank；The blending tank
Outlet is connected with first-stage reactor tube side import；The import of the heating tank is connect with the outlet of condensation collection sulphur device；
Catalyst is filled in the first-stage reactor tube side；
The cooling recovery unit includes sequentially connected condenser and catches sulphur device；The outlet of the second reactor with
The import of condenser is connected.
Above-mentioned selective oxidation sulfur recovery facility further includes drum；The shell of the tube side outlet and first-stage reactor of the drum
Journey import is connected；The shell-side outlet of the first-stage reactor is connected with the tube side import of drum；The shell-side outlet of the drum with
The shell side import of heating tank is connected.
Above-mentioned selective oxidation sulfur recovery facility further include be arranged in condensation collection sulphur device outlet and second reactor into
Go into operation heater and heat exchanger between mouthful；The outlet of the condensation collection sulphur device is divided into three branches；The first branch is cold
The outlet heater that gone into operation of agglutination sulphur device is connected with the import of second reactor；The second branch is bypass；The third
Branch is that the outlet of second reactor is connected through heat exchanger with condenser inlet, at the same condense the outlet of collection sulphur device through heat exchanger with
Condenser inlet is connected.
Having heaters is set on the above-mentioned export pipeline for catching sulphur device.
There is angle between the central axis and horizontal line of above-mentioned waste heat boiler；The angle is 5~15 °.
A kind of recovery process of selective oxidation sulfur recovery facility, which is characterized in that the isothermal selective oxidation sulphur returns
Skill of knocking off the following steps are included:
1) mixed gas
Hydrogen sulfide gas is sent into heating after cure hydrogen in heating tank through blower and enters mixing after knockout drum separates
In tank, and with the oxygen mix that is passed directly into blending tank, obtain mixed gas；
2) level-one isothermal Selective Oxidation
Mixed gas enters in first-stage reactor from first-stage reactor tube side import, under the effect of the catalyst mixed gas
Isothermal Selective Oxidation occurs, obtains primary first-order equation processed gas；
It is connected by the tube side outlet of drum with the shell side import of first-stage reactor in isothermal Selective Oxidation, level-one
The shell-side outlet of reactor is connected with the tube side import of drum, so that the temperature in first-stage reactor is at 140~350 DEG C, thus
Mixed gas carries out isothermal Selective Oxidation；
3) cooling
Primary first-order equation processed gas enters waste heat boiler and is cooled down, and obtains useless pot processed gas；
4) it condenses
Useless pot processed gas enters condensation in condensation collection sulphur device and obtains molten sulfur and a condensed gas, and molten sulfur collects from condensation
Sulphur device outlet at bottom enters sulphur pond；The condensed gas come out from condensation collection sulphur device top exit is divided into two-way, is all the way
Reaction gas as recyclegas return heating tank in after hydrogen sulfide and oxygen mix enter the first-stage reactor stage, execute step
2)；
Another way is that the non-reaction gas that unstripped gas is brought into enters the secondary response stage, executes step 5)；
5) secondary response
The another way come out from condensation collection sulphur device top exit is laggard as the secondary response mixed gas heater that gone into operation
Enter and carries out secondary response in second reactor；
6) time condensation
The secondary response processed gas come out from second reactor, enters in condenser after heat exchanger and is condensed,
Obtain time condensation gas and liquid-state sulfur；Liquid-state sulfur enters sulphur pond from condenser outlet at bottom；
6) Recovered sulphur
The time condensation gas come out from condenser overhead, which enters, catches further Recovered sulphur in sulphur device, obtains desulfidation tail gas
And liquid-state sulfur；Desulfidation tail gas enters boiler or oxidation catalysis after heat exchanger and handles, and liquid-state sulfur is from catching sulphur device bottom
Portion outlet enters sulphur pond.
Above-mentioned steps 1) in the concentration of hydrogen sulfide gas be 3%~98%.
Above-mentioned steps 1) in mixed gas the volume ratio of oxygen and hydrogen sulfide gas be 0.3~0.9.
Above-mentioned steps 2) in the catalyst that loads in first-stage reactor be Ti-base catalyst.
Above-mentioned steps 6) in catch sulphur device catch sulphur temperature control at 130~170 DEG C.
The beneficial effects of the present invention are:
1, selective oxidation sulfur recovery facility provided by the invention, it is gaseous mixture unit, first-stage reactor, waste heat boiler, cold
It is aggregated sulphur device, second reactor and cooling recovery unit；Tube side of the outlet of gaseous mixture unit through first-stage reactor and useless
The tube side of heat boiler is finally connected with the import of condensation collection sulphur device；Condensation collection sulphur device outlet respectively with gaseous mixture unit inlet with
And the import of second reactor is connected；The outlet of second reactor is connected with cooling recovery unit.The equipment that the present invention uses compared with
It is few, it invests small.
2, the present invention is filled with Ti-base catalyst in first-stage reactor tube side；The reaction temperature of first-stage reactor is 140
~350 DEG C, and the shell side of first-stage reactor is connected with drum and forms boiler water cycle system, so that anti-in first-stage reactor
Temperature is answered to be maintained at constant temperature, it is easy to operate, increase the efficiency of desulfurization.
3, first order reaction processed gas of the present invention generates a condensed gas after waste heat boiler and condensation collection sulphur device,
The reaction gas that unstripped gas in condensed gas brings system into be formed mixing as recyclegas with hydrogen sulfide and oxygen
Gas enters first-stage reactor reaction, and the non-reaction gas that raw material is brought into is into discharging after second order reaction, so that the desulfuration efficiency of technique
It is further enhanced.
4, the desulfurization that selective oxidation sulfur recovery facility provided by the invention is suitable for the hydrogen sulfide gas of various concentration is returned
It receives, has a wide range of application, and sulfur recovery rate is high, operating cost is low.
Detailed description of the invention
Fig. 1 isothermal selective oxidation recovery technology of sulfur flow diagram provided by the invention；
Wherein:
R001-first-stage reactor；R002-second reactor；V001-knockout drum；V002-blending tank；V003-vapour
Packet；E001-heating tank；E002-waste heat boiler；E003-condenser；E004-catches sulphur device；E005-condensation collection sulphur device；
E006-goes into operation heater；E007-heat exchanger；E008-heater；C001-blower；C002-circulating fan；
1-hydrogen sulfide gas；2-oxygen gas；3-mixed gas；4-primary first-order equation processed gas；5-useless pot desulfurization
Gas；6-condensed gas；7-recyclegas；8-secondary response mixed gas；9-secondary response processed gas；10—
Time condensation gas；11-desulfidation tail gas；12-middle pressure steams；13-boiler waters；14-waste liquids.
Specific embodiment
Now in conjunction with attached drawing and embodiment, the present invention will be described in detail.
Referring to Fig. 1, selective oxidation sulfur recovery facility provided by the invention, including gaseous mixture unit, first-stage reactor
R001, waste heat boiler E002, condensation collection sulphur device E005, second reactor R002 and cooling recovery unit.Gaseous mixture unit
The tube side for exporting tube side and waste heat boiler E002 through first-stage reactor R001 finally collects the import phase of sulphur device E005 with condensation
Even, the outlet of condensation collection sulphur device E005 is connected with the import of gaseous mixture unit inlet and second reactor R002 respectively, second level
The outlet of reactor R002 is connected with cooling recovery unit；Gaseous mixture unit includes sequentially connected knockout drum V001, blower
The outlet of C002, heating tank E001 and blending tank V002, blending tank V002 are connected with first-stage reactor R001 tube side import, cold
The outlet of agglutination sulphur device E005 is connected with the import of heating tank E001 and the import of second reactor R002 respectively；Waste heat boiler
There is angle between the central axis and horizontal line of E002；Angle is 5~15 °, so that primary first-order equation processed gas 4 is through waste heat boiler
E002 molten sulfur after cooling enters in condensation collector E005 together with useless pot processed gas 5, and molten sulfur will not be in waste heat boiler
It remains or carries secretly on E002 inner wall；Cooling recovery unit includes sequentially connected condenser E003 and catches sulphur device E004, second level
The outlet of reactor R002 successively with condenser E003 and catch sulphur device E004 and be connected.First-stage reactor R001 is shell-and-tube reaction
Device is filled with catalyst in tube side, and catalyst is Ti-base catalyst.Second reactor R002 is adiabatic condensation reactor.
Selective oxidation sulfur recovery facility provided by the invention further includes drum V003；The tube side outlet and one of drum V003
The shell side import of stage reactor R001 is connected；The shell-side outlet of first-stage reactor R001 is connected with the tube side import of drum V003；
The shell-side outlet of drum V003 is connected with the shell side import of heating tank E001.
Selective oxidation sulfur recovery facility provided by the invention further includes the outlet and two that condensation collection sulphur device E005 is arranged in
The heater E006 and heat exchanger E007 that goes into operation between the import of stage reactor R002；The outlet of condensation collection sulphur device E005 is divided into three
A branch；The first branch is the outlet of condensation collection sulphur device E005 through the import phase for the heater E006 and second reactor R002 that goes into operation
Even；Second branch is bypass；Third branch is the outlet of second reactor R002 through heat exchanger E007 and condenser E003 import
It is connected, while the outlet for condensing collection sulphur device E005 is connected with condenser E003 import.It catches and is arranged on the export pipeline of sulphur device E004
Having heaters E008.
The recovery process of isothermal selective oxidation sulphur provided by the invention, comprising the following steps:
1) 3%~98% hydrogen sulfide gas 1 is sent into heating tank E001 through blower C001 after knockout drum V001 separation
Middle heating, be heated to certain temperature hydrogen sulfide gas 1 enter blending tank V002 in, and be passed directly into blending tank V002
Oxygen 2 mixes, and obtains mixed gas 3, and the volume ratio of oxygen 2 and hydrogen sulfide gas 1 is 0.3~0.9 in mixed gas 3；
2) mixed gas 3 enters in first-stage reactor R001 from first-stage reactor R001 tube side import, Ti-base catalyst,
Isothermal Selective Oxidation occurs in first-stage reactor R001 for mixed gas 3 at 140~350 DEG C of reaction temperature, obtains primary
Reaction desulfuration gas 4；When carrying out isothermal Selective Oxidation in successively reactor R001, the tube side outlet and one of drum V003
The shell side import of stage reactor R001 is connected, and the shell-side outlet of first-stage reactor R001 is connected with the tube side import of drum V003,
So that the temperature in first-stage reactor R001 is maintained within the scope of 140~350 DEG C, so that mixed gas 3, which carries out isothermal, selects oxygen
Change reaction；The shell-side outlet of drum V003 is connected with the shell side import of heating tank E001, and the middle pressure that drum V003 shell side comes out is steamed
Vapour can be heated or be supplied other desired boiler to the gas in heating tank E001；
3) primary first-order equation processed gas 4 is cooled down into waste heat boiler E002, obtains useless pot processed gas 5；
4) the pot processed gas 5 that gives up enters condensation in condensation collection sulphur device E005 and obtains molten sulfur and a condensed gas 6, molten sulfur
Sulphur pond is entered from condensation collection sulphur device E005 outlet at bottom；Condensed gas 5 comes out from condensation collection sulphur device E005 top exit
After be divided into two-way, containing reaction gas all the way as recyclegas 7 by circulating fan C002 return heating tank E001 in sulphur
Enter first-stage reactor reaction R001 circular response, in the specific implementation, circulating air after changing hydrogen 1 and the mixing of oxygen gas 2
The internal circulating load of body determines jointly according to the sulphur concentration in the sulphur concentration and recyclegas in unstripped gas, to guarantee the recycling effect of sulphur
Rate；Another way unstripped gas, which brings the non-reaction gas of system into and gone into operation as secondary response mixed gas 8, to be entered after heater E006
Secondary response is carried out in second reactor R002；
5) the secondary response processed gas 9 come out from second reactor R002 enters condenser after heat exchanger E007
It is condensed in E003, obtains time condensation gas 10 and liquid-state sulfur；Liquid-state sulfur from condenser E003 outlet at bottom into
Enter sulphur pond；
6) the time condensation gas 10 come out at the top of condenser E003, which enters, catches further Recovered sulphur in sulphur device E004,
Desulfidation tail gas 11 and liquid-state sulfur can be obtained at 130~170 DEG C by catching the control of sulphur temperature；Desulfidation tail gas 11 is by heating it
Enter boiler or oxidation catalysis processing after E008 until qualified discharge, liquid-state sulfur enter sulphur from sulphur device E004 outlet at bottom is caught
Pond.
Embodiment 1
First-stage reactor R001 provided by the invention is shell-and-tube reactor, and second reactor R002 is the cold tube reaction of adverse current
Device, the angle between the central axis and horizontal line of waste heat boiler E002 are 10 °.
When carrying out sulphur recovery processing using selective oxidation sulfur recovery facility provided by the invention, hydrogen sulfide gas 1
Concentration is 35%, and the concentration of oxygen gas 2 is 99.6%, and the volume ratio of oxygen and hydrogen sulfide gas is 0.3, by blending tank
Enter in first-stage reactor R001 after V002 mixing, the temperature in first-stage reactor R001 is 140 DEG C, catches sulphur device E004 temperature control
System is at 130 DEG C, and after first-stage reactor R001 and second reactor R002, the rate of recovery of sulphur is 98.6%, desulfurization tail
Sulfur content in gas 11 is 400mg/L, and desulfidation tail gas 11 returns to low-temp methanol after pressurizeing and washes reprocessing；But desulfidation tail gas amount compared with
It is few, therefore required power consumption is few.
Embodiment 2
Unlike the first embodiment, the angle between the central axis and horizontal line of waste heat boiler E002 is 5 °, hydrogen sulfide
The concentration of gas 1 is 50%, and the concentration of oxygen gas 2 is 99.6%, and the volume ratio of oxygen and hydrogen sulfide gas is 0.42, is passed through
Enter in first-stage reactor R001 after blending tank V002 mixing, the temperature in first-stage reactor R001 is 205 DEG C, catches sulphur device E004
Temperature is controlled at 150 DEG C, after first-stage reactor R001 and second reactor R002, the rate of recovery of sulphur 98.4%,
Sulfur content in desulfidation tail gas 11 is 300mg/L；Desulfidation tail gas 11 returns to boiler and is handled.
Embodiment 3
Unlike the first embodiment, the angle between the central axis and horizontal line of waste heat boiler E002 is 15 °, vulcanization
The concentration of hydrogen 1 is 3%, and the concentration of oxygen gas 2 is 99.6%, and the volume ratio of oxygen and hydrogen sulfide gas is 0.9, is passed through
Enter in first-stage reactor R001 after blending tank V002 mixing, the temperature in first-stage reactor R001 is 340 DEG C, catches sulphur device E004
Temperature is controlled at 170 DEG C, and after first-stage reactor R001 and second reactor R002, the rate of recovery of sulphur takes off 99%
Sulfur content in sulphur tail gas 11 is 120mg/L；11 qualified discharge of desulfidation tail gas.
Embodiment 4
As different from Example 3, the angle between the central axis and horizontal line of waste heat boiler E002 is 8 °, hydrogen sulfide
The concentration of gas 1 is 98%, and the concentration of oxygen gas 2 is 99.6%, and the volume ratio of oxygen and hydrogen sulfide gas is 0.62, is passed through
Enter in first-stage reactor R001 after blending tank V002 mixing, the temperature in first-stage reactor R001 is 265 DEG C, catches sulphur device E004
Temperature is controlled at 140 DEG C, and after first-stage reactor R001 and second reactor R002, the rate of recovery of sulphur takes off 98%
Sulfur content in sulphur tail gas 11 is 700mg/L；Desulfidation tail gas 11 returns to low-temp methanol after pressurizeing and washes reprocessing；But desulfidation tail gas
It is few to measure less therefore required power consumption.
Embodiment 5
Unlike the first embodiment, the angle between the central axis and horizontal line of waste heat boiler E002 is 5 °, hydrogen sulfide
The concentration of gas 1 is 75%, and the concentration of oxygen gas 2 is 99.6%, and the volume ratio of oxygen and hydrogen sulfide gas is 0.75, is passed through
Enter in first-stage reactor R001 after blending tank V002 mixing, the temperature in first-stage reactor R001 is 255 DEG C, catches sulphur device E004
Temperature is controlled at 160 DEG C, and after first-stage reactor R001 and second reactor R002, the rate of recovery of sulphur takes off 98%
Sulfur content in sulphur tail gas 11 is 500mg/L；Desulfidation tail gas 11 returns to boiler and is handled.
Claims (10)
1. a kind of selective oxidation sulfur recovery facility, which is characterized in that the selective oxidation sulfur recovery facility includes gaseous mixture
Unit, first-stage reactor (R001), waste heat boiler (E002), condensation collection sulphur device (E005), second reactor (R002) and cold
But recovery unit；The pipe of tube side and waste heat boiler (E002) of the outlet of the gaseous mixture unit through first-stage reactor (R001)
Journey is finally connected with the import of condensation collection sulphur device (E005)；It is described condensation collection sulphur device (E005) outlet respectively with gaseous mixture unit
Import and second reactor (R002) import be connected；The outlet of the second reactor (R002) and cooling recovery unit
It is connected；
The gaseous mixture unit includes sequentially connected knockout drum (V001), blower (C001), heating tank (E001) and mixing
Tank (V002)；The outlet of the blending tank (E001) is connected with first-stage reactor (R001) tube side import；The heating tank
(E001) import is connect with the outlet of condensation collection sulphur device (E005)；
Catalyst is filled in first-stage reactor (R001) tube side；
The cooling recovery unit includes sequentially connected condenser (E003) and catches sulphur device (E004)；The condenser
(E003) import is connected with the outlet of second reactor (R002).
2. selective oxidation sulfur recovery facility according to claim 1, which is characterized in that the selective oxidation sulphur recovery
Device further includes drum (V003)；The tube side outlet of the drum (V003) is connected with the shell side import of first-stage reactor；It is described
The tube side import of drum (V003) is connected with the shell-side outlet of first-stage reactor (R001)；The shell-side outlet of the drum (V003)
It is connected with the shell side import of heating tank (E001).
3. selective oxidation sulfur recovery facility according to claim 2, which is characterized in that the selective oxidation sulphur recovery
Device further includes go into operation heating of the setting between the outlet of condensation collection sulphur device (E005) and the import of second reactor (R002)
Device (E006) and heat exchanger (E007)；The outlet of condensation collection sulphur device (E005) is divided into three branches；The first branch is
The outlet of condensation collection sulphur device (E005) is connected through the heater that goes into operation (E006) with the import of second reactor (R002)；Described second
Branch is bypass；The third branch be second reactor (R002) outlet through heat exchanger (E007) and condenser (E003) into
Mouth is connected, and the outlet of condensation collection sulphur device (E005) is connected through heat exchanger (E007) with condenser (E003) import.
4. selective oxidation sulfur recovery facility according to claim 3, which is characterized in that described to catch going out for sulphur device (E004)
Having heaters (E008) is set on mouth pipeline.
5. selective oxidation sulfur recovery facility according to claim 1 or 2 or 3 or 4, which is characterized in that the waste heat boiler
There is angle between the central axis and horizontal line of furnace (E002)；The angle is 5~15 °.
6. a kind of recovery process of selective oxidation sulfur recovery facility as described in claim 1, which is characterized in that the isothermal
Selective oxidation recovery technology of sulfur the following steps are included:
1) mixed gas
Hydrogen sulfide gas is sent into heating tank (E001) through blower after knockout drum (V001) separation and heats after cure hydrogen
Into in blending tank (V002), and with the oxygen mix that is passed directly into blending tank (V002), obtain mixed gas；
2) level-one isothermal Selective Oxidation
Mixed gas enters in first-stage reactor (R001) from first-stage reactor (R001) tube side import, under the effect of the catalyst
Isothermal Selective Oxidation occurs for mixed gas, obtains primary first-order equation processed gas；
Tube side in isothermal Selective Oxidation through drum (V003) exports the shell side import with first-stage reactor (R001)
It is connected, the shell-side outlet of first-stage reactor (R001) is connected with the tube side import of drum (V003), so that first-stage reactor
(R001) temperature in is at 140~350 DEG C, so that mixed gas carries out isothermal Selective Oxidation；
3) cooling
Primary first-order equation processed gas enters waste heat boiler (E002) and is cooled down, and obtains useless pot processed gas；
4) it condenses
Useless pot processed gas enters condensation in condensation collection sulphur device (E005) and obtains molten sulfur and a condensed gas, and molten sulfur is from condensation
Collection sulphur device (E005) outlet at bottom enters sulphur pond；Condensed gas divides after coming out from condensation collection sulphur device (E005) top exit
At two-way, it is used as in recyclegas return heating tank (E001) all the way and enters first order reaction rank after hydrogen sulfide and oxygen mix
Section executes step 2)；
Another way enters the secondary response stage, executes step 5)；
5) secondary response
The another way come out from condensation collection sulphur device (E005) top exit is as secondary response mixed gas through the heater that goes into operation
(E006) enter afterwards and carry out secondary response in second reactor (R002)；
6) time condensation
The secondary response processed gas come out from second reactor (R002), enters condenser after heat exchanger (E007)
(E003) it is condensed in, obtains time condensation gas and liquid-state sulfur；Liquid-state sulfur is from condenser (E003) outlet at bottom
Into sulphur pond；
6) Recovered sulphur
The time condensation gas come out at the top of from condenser (E003), which enters, catches further Recovered sulphur in sulphur device (E004), obtains
Desulfidation tail gas and liquid-state sulfur；Desulfidation tail gas enters boiler after heat exchanger (E007) or oxidation catalysis is handled, liquid
Sulphur enters sulphur pond from sulphur device (E004) outlet at bottom is caught.
7. the recovery process of selective oxidation sulfur recovery facility according to claim 6, which is characterized in that the step 1)
The concentration of middle hydrogen sulfide gas is 3%~98%.
8. the recovery process of selective oxidation sulfur recovery facility according to claim 7, which is characterized in that the step 1)
The volume ratio of oxygen and hydrogen sulfide gas is 0.3~0.9 in middle mixed gas.
9. the recovery process of selective oxidation sulfur recovery facility according to claim 8, which is characterized in that the step 2)
The catalyst loaded in middle first-stage reactor (R001) is Ti-base catalyst.
10. the recovery process of selective oxidation sulfur recovery facility according to claim 9, which is characterized in that the step
6) the sulphur temperature of catching that sulphur device (E004) is caught in is controlled at 130~170 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910735975.1A CN110329995A (en) | 2019-08-09 | 2019-08-09 | Selective oxidation sulfur recovery facility and recovery process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910735975.1A CN110329995A (en) | 2019-08-09 | 2019-08-09 | Selective oxidation sulfur recovery facility and recovery process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110329995A true CN110329995A (en) | 2019-10-15 |
Family
ID=68148996
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910735975.1A Pending CN110329995A (en) | 2019-08-09 | 2019-08-09 | Selective oxidation sulfur recovery facility and recovery process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110329995A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101117214A (en) * | 2007-04-30 | 2008-02-06 | 中国石油集团工程设计有限责任公司 | Improved low-temperature Claus sulfur recovery method |
| CN102556977A (en) * | 2010-12-30 | 2012-07-11 | 中国石油天然气股份有限公司 | Inner cooling type direct oxidation recycling method and recycling device of sulfur |
| CN204643846U (en) * | 2015-01-19 | 2015-09-16 | 西安长庆科技工程有限责任公司 | A kind of Gas Purification Factory low-sulfur high-carbon acid gas sulfur recovery unit |
| CN109019524A (en) * | 2018-08-30 | 2018-12-18 | 山东迅达化工集团有限公司 | A kind of recovery technology of sulfur of middle low concentration sour gas |
-
2019
- 2019-08-09 CN CN201910735975.1A patent/CN110329995A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101117214A (en) * | 2007-04-30 | 2008-02-06 | 中国石油集团工程设计有限责任公司 | Improved low-temperature Claus sulfur recovery method |
| CN102556977A (en) * | 2010-12-30 | 2012-07-11 | 中国石油天然气股份有限公司 | Inner cooling type direct oxidation recycling method and recycling device of sulfur |
| CN204643846U (en) * | 2015-01-19 | 2015-09-16 | 西安长庆科技工程有限责任公司 | A kind of Gas Purification Factory low-sulfur high-carbon acid gas sulfur recovery unit |
| CN109019524A (en) * | 2018-08-30 | 2018-12-18 | 山东迅达化工集团有限公司 | A kind of recovery technology of sulfur of middle low concentration sour gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102942162B (en) | Liquid-phase treatment process of tail gas from sulfur recovery | |
| CN105521687B (en) | A method of utilizing coal tar hydrogenating hydrogen sulfide gas by-product sulphur | |
| CN103041679A (en) | Waste gas treatment system of acid gas containing ammonia | |
| CN102205202A (en) | Processing method for acid gas containing H2S | |
| CN104843650B (en) | A kind of Gas Purification Factory low-sulfur high-carbon acid gas sulfur recovery technology and device | |
| CN101626977A (en) | Process for the production of sulfuric acid | |
| CN211521596U (en) | System for preparing analytically pure sulfuric acid from smelting flue gas | |
| CN103318850A (en) | Low-temperature waste heat recovery system for pyrite and metallurgical off-gas acid making device | |
| CN110240164A (en) | The method and device of fluosilicic acid concentration | |
| CN103318847A (en) | High-efficiency sulfur recovery method of waste gas containing hydrogen sulfide | |
| CN105348145B (en) | The method of ammonia type flue gas desulfurizing by-product cyclohexanone oxime | |
| US3374061A (en) | Process for obtaining sulfuric acid | |
| CN113274755A (en) | Process and device for preparing oxygen by phase thermal decomposition of sulfuric acid in iodine-sulfur cycle | |
| CN106800276B (en) | Utilize the industrialized preparing process of sterling sulfur trioxide vapor- phase synthesis chlorosulfonic acid | |
| CN106731582A (en) | A kind of method of integrated treatment sulfide hydrogen acid waste gas and solid waste carnallite | |
| CN101239705A (en) | Method for obtaining high-purity sulfur from gas containing hydrogen sulfide | |
| CN110329995A (en) | Selective oxidation sulfur recovery facility and recovery process | |
| CN204412040U (en) | A kind of combined type Gas Purification Factory low concentration acid gas processing device | |
| US2003442A (en) | Manufacture of sulphuric acid from hydrogen sulphide gas | |
| CN106672904A (en) | Method for comprehensively treating sulfur-containing flue gas and solid waste abraum salt | |
| CN101565172A (en) | Method for recovering sulfur from byproduct of acid gas generated in production of rubber chemicals | |
| CN105727714B (en) | A kind of process and device for producing NaHS | |
| CN210528467U (en) | Selective oxidation sulfur recovery device | |
| CN101389568B (en) | Method of optimizing the operation of claus units | |
| CN209702624U (en) | The parallel methanol synthesis reaction system of double-reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |