CN106915727A - Liquid sulfur degassing process - Google Patents
Liquid sulfur degassing process Download PDFInfo
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- CN106915727A CN106915727A CN201510993224.1A CN201510993224A CN106915727A CN 106915727 A CN106915727 A CN 106915727A CN 201510993224 A CN201510993224 A CN 201510993224A CN 106915727 A CN106915727 A CN 106915727A
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- tail gas
- gas
- molten sulfur
- degasification
- delivered
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 171
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 118
- 239000011593 sulfur Substances 0.000 title claims abstract description 118
- 238000007872 degassing Methods 0.000 title claims abstract description 99
- 239000007788 liquid Substances 0.000 title claims abstract description 74
- 239000007789 gas Substances 0.000 claims abstract description 182
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 84
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 52
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 42
- 230000023556 desulfurization Effects 0.000 claims abstract description 28
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 20
- 230000005587 bubbling Effects 0.000 claims abstract description 20
- 239000003546 flue gas Substances 0.000 claims abstract description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000000034 method Methods 0.000 claims description 72
- 239000005864 Sulphur Substances 0.000 claims description 56
- 238000005984 hydrogenation reaction Methods 0.000 claims description 45
- 230000003009 desulfurizing effect Effects 0.000 claims description 35
- 230000008569 process Effects 0.000 claims description 16
- 238000011084 recovery Methods 0.000 claims description 14
- 238000002485 combustion reaction Methods 0.000 claims description 12
- 230000008929 regeneration Effects 0.000 claims description 12
- 238000011069 regeneration method Methods 0.000 claims description 12
- 239000002918 waste heat Substances 0.000 claims description 9
- 150000002898 organic sulfur compounds Chemical class 0.000 claims description 8
- 239000003517 fume Substances 0.000 claims description 2
- 230000007062 hydrolysis Effects 0.000 claims description 2
- 238000006460 hydrolysis reaction Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 16
- 230000000694 effects Effects 0.000 abstract description 11
- 150000003568 thioethers Chemical class 0.000 abstract description 3
- 238000012545 processing Methods 0.000 abstract description 2
- 238000006902 nitrogenation reaction Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 45
- 238000006243 chemical reaction Methods 0.000 description 10
- 230000003301 hydrolyzing effect Effects 0.000 description 8
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 7
- 230000001105 regulatory effect Effects 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 230000000903 blocking effect Effects 0.000 description 2
- 238000005202 decontamination Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000001939 inductive effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
- 238000004073 vulcanization Methods 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
- C01B17/0232—Purification, e.g. degassing
-
- 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
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a liquid sulfur degassing process, and belongs to the technical field of gas processing. The liquid sulfur degassing process comprises the following steps: introducing a mixed gas of nitrogen and desulfurization tail gas from a desulfurization tower into a liquid sulfur pool, and bubbling liquid sulfur at 140-160 ℃ to make sulfide in the liquid sulfur enter a gas phase to obtain degassed liquid sulfur and liquid sulfur degassing tail gas; the volume percentage of the desulfurization tail gas from the desulfurization tower in the mixed gas is 20-60%. The liquid sulfur degassing process can effectively remove sulfides in the liquid sulfur to enable the content of the sulfides in the liquid sulfur to be below 10ppm, can also obviously reduce the energy consumption in the liquid sulfur degassing process and the treatment of tail gas generated by the liquid sulfur degassing, and can also obviously reduce the SO in the flue gas discharged after the tail gas generated by the liquid sulfur degassing is treated2The content of (A) can reach 80mg/m3In the following, good energy-saving and emission-reducing effects are achieved.
Description
Technical field
The present invention relates to gas processing technique field, more particularly to a kind of liquid sulphur degasification technique.
Background technology
In petroleum chemical industry, generally using Crouse's (Claus) sulfur recovery facility by natural gas, refining
Contained H in factory's gas and synthesis gas2S sulfides are in the form of liquid elemental sulphur (hereinafter referred to as molten sulfur)
Reclaim.A certain amount of sulfide, including H are dissolved with the molten sulfur of claus plant production2S with
And COS, CS2Deng organic sulfur compound.During molten sulfur conveying, storage and use, above-mentioned sulfide can be analysed
Go out and cause the corrosion of systematic pipeline, equipment；When can be exploded when confined space accumulates to finite concentration,
Security incident and personnel are caused to injure.Therefore, in order to reduce molten sulfur conveying, storage and use during
Potential safety hazard, prevents the pollution of the environment with economic loss, it is necessary to by the sulfide removing in molten sulfur, remove molten sulfur
The process of middle sulfide is also referred to as molten sulfur degasification process.
Conventional liquid sulphur degasification technique mainly has Shell degasification techniques, Aquisulf degasification techniques, Exxon at present
Degasification technique, Amoco (BP) degasification technique, D ' GAASS degasification techniques and HySpec degasification techniques
Deng.Above-mentioned liquid sulphur degasification technique is mainly using air as source of the gas, the sulfide in molten sulfur is entered gas phase
The tail gas that deaerates is obtained, the master of claus plant is transmitted back to after degassing tail gas compressor compresses again
Combustion furnace carries out claus reaction.The tail gas of claus plant is hydrogenated with into hydrogenation reactor
Reduction reaction, makes organic sulfur compound be converted into H2S is obtained being hydrogenated with tail gas, and hydrogenation tail gas is delivered into desulfurizing tower
Carry out solution desulfurization and obtain desulfidation tail gas, desulfidation tail gas are discharged by after incinerator burning.This method energy consumption
It is higher, pipeline blocking is easily caused, can also influence claus plant air distribution to cause plant running unstable
It is fixed.The desulfidation tail gas that also document report obtains solution desulfurization are used as the source of the gas of molten sulfur degasification, and what is obtained is de-
Tail-gas are into hydrogenation reactor and then carry out solution desulfurization again.This method is also required to compressor or larger
The air-introduced machine of power, energy consumption is higher, and produces in degassing tail gas containing a large amount of CO2, it is recycled into desulfurization
The internal circulating load of desulfuration solution and the regeneration energy consumption of desulfuration solution can be increased after tower.
To sum up, realize it is of the invention during, inventor find prior art at least there is problems with：
Existing liquid sulphur degasification technique high energy consumption.
The content of the invention
In order to solve the above-mentioned technical problem, to provide a kind of energy consumption low and can effectively remove molten sulfur for the present invention
The liquid sulphur degasification technique of sulfide.
Specifically, including following technical scheme：
A kind of liquid sulphur degasification technique, the liquid sulphur degasification technique includes：
The mixed gas of nitrogen and the desulfidation tail gas from desulfurizing tower are passed through in molten sulfur pond, at 140 DEG C~160 DEG C
Under the conditions of bubbling is carried out to molten sulfur, sulfide in molten sulfur is obtained deaerate molten sulfur and molten sulfur degasification into gas phase
Tail gas；The percent by volume of the desulfidation tail gas from desulfurizing tower described in the mixed gas is 20%~60%.
Preferably, the percent by volume of the desulfidation tail gas from desulfurizing tower is described in the mixed gas
30%~50%.
Preferably, the percent by volume of the desulfidation tail gas from desulfurizing tower is described in the mixed gas
35%~45%.
Further, the nitrogen comes from air-separating plant.
Further, the liquid sulphur degasification technique also includes：
The molten sulfur degasification tail gas is delivered in hydrogenation reactor and is hydrogenated with the conditions of 230 DEG C~240 DEG C
Hydrolysis, makes the organic sulfur compound in the molten sulfur degasification tail gas be converted into H2S obtains being hydrogenated with tail gas；
The hydrogenation tail gas is delivered to carry out solution desulfurization and obtains the desulfidation tail gas in the desulfurizing tower；Institute
State in solution sweetening process, temperature when the poor absorbing liquid of desulfurization enters the desulfurizing tower is 30 DEG C~40 DEG C；
A part of desulfidation tail gas are delivered to the molten sulfur pond, desulfidation tail gas described in another part are conveyed
To incinerator burn and obtain flue gas, and by the fume emission.
Further, the molten sulfur degasification tail gas is delivered in hydrogenation reactor using jet pump, the spray
The steam pressure for penetrating pump is 500KPa~700KPa.
Further, the molten sulfur degasification tail gas is delivered to after line combustion furnace and is delivered to the hydrogenation again instead
In answering device.
Further, the hydrogenation tail gas is delivered into waste heat boiler carries out heat recovery, then is delivered to chilling
Tower cooler carries out solution desulfurization to being delivered in the desulfurizing tower after 35 DEG C~45 DEG C.
Further, in the solution sweetening process, desulfuration solution internal circulating load is 70~85m3/ h, desulfuration solution
Regeneration steam consumption is 7.0~8.5t/h.
The beneficial effect of technical scheme provided in an embodiment of the present invention is：
Liquid sulphur degasification technique provided in an embodiment of the present invention is excellent by carrying out to source of the gas used in the process of molten sulfur degasification
Change and improve, on the one hand ensure that the effect of molten sulfur degasification, molten sulfur is de-gassed using the technique on the other hand
The molten sulfur degasification tail gas for obtaining afterwards is easily purified, and advantageously reduces energy consumption.In the embodiment of the present invention, with
The mixed gas of nitrogen and the desulfidation tail gas from desulfurizing tower are used as bubbling source of the gas.Desulfidation tail gas are used with whole
Compared as bubbling source of the gas, CO in the mixed gas2Content is relatively low, when the method for use solution desulfurization is to liquid
When stream degassing tail gas carries out follow-up purified treatment, CO can be reduced2Competition absorb, significantly improve desulfurization
The desulfurized effect of solution, while steam consumption when also reducing desulfuration solution internal circulating load and desulfuration solution regeneration,
With good effects of energy saving and emission reduction.Compared with molten sulfur degasification bubbling source of the gas is used air as, the gaseous mixture
It is not oxygenous in body, on the premise of molten sulfur degasification effect is ensured, it is to avoid to combustion furnace of sulfur recovery device
Air distribution than influence, reduce sulfur recovery facility fluctuation make its even running, advantageously reduce energy consumption.And
Compared with all employing nitrogen as bubbling source of the gas, it is possible to reduce nitrogen use level, when utilizing air-separating plant
When nitrogen is provided, the load of air-separating plant can be significantly reduced, save electric energy.To sum up, using this hair
The technique that bright embodiment is provided is removed to the sulfide in molten sulfur, can make the matter of the sulfide in molten sulfur
Amount concentration reaches below 10ppm, and significantly reduces energy consumption.
Brief description of the drawings
Technical scheme in order to illustrate more clearly the embodiments of the present invention, institute in being described to embodiment below
The accompanying drawing for needing to use is briefly described, it should be apparent that, drawings in the following description are only the present invention
Some embodiments, for those of ordinary skill in the art, on the premise of not paying creative work,
Other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is the flow chart of liquid sulphur degasification technique provided in an embodiment of the present invention.
Reference is represented respectively：
1st, molten sulfur pond；2nd, bubbler；3rd, nitrogen flow regulating valve；4th, nitrogen stream scale；
5th, liquid sulfur pump；6th, jet pump；7th, online combustion furnace；8th, hydrogenation reactor；
9th, waste heat boiler；10th, chilling tower；11st, desulfurizing tower；12nd, air-introduced machine；
13rd, desulfidation tail gas flow control valve；14th, desulfidation tail gas flowmeter；15th, incinerator；
16th, chimney；
A, molten sulfur；B, low-pressure steam；C, condensate；D, nitrogen；E, mixed gas；
F, de- gas-liquid flow；G, injection steam；H, molten sulfur degasification tail gas；The tail gas of i, sulfur recovery facility；
J, waste heat boiler institute producing steam；K, hydrogenation tail gas；M, desulfidation tail gas；N, flue gas.
Specific embodiment
To make technical scheme and advantage clearer, below in conjunction with accompanying drawing to embodiment party of the present invention
Formula is described in further detail.
The embodiment of the present invention provides a kind of liquid sulphur degasification technique, and referring to Fig. 1, the liquid sulphur degasification technique includes：
The mixed gas e of nitrogen d and the desulfidation tail gas m from desulfurizing tower 11 is passed through in molten sulfur pond 1,
Bubbling is carried out to molten sulfur under the conditions of 140 DEG C~160 DEG C, the sulfide in molten sulfur is obtained the molten sulfur that deaerates into gas phase
F and molten sulfur degasification tail gas h；The percent by volume of the desulfidation tail gas m from desulfurizing tower is in mixed gas
20%~60%.
The embodiment of the present invention optimizes improvement by source of the gas used in the process of molten sulfur degasification, has obtained one kind
The liquid sulphur degasification technique that degasifying effect is good, energy consumption is low.In liquid sulphur degasification technique provided in an embodiment of the present invention,
Using nitrogen and the mixed gas of the desulfidation tail gas from desulfurizing tower 11 remove sulphur in molten sulfur as bubbling source of the gas
Compound.With all using desulfidation tail gas as bubbling source of the gas compared with, CO in the mixed gas2Content is relatively low,
When the method using solution desulfurization carries out follow-up purified treatment to liquid stream degassing tail gas, CO can be reduced2
Competition absorb, significantly improve the desulfurized effect of desulfuration solution, at the same also reduce desulfuration solution internal circulating load and
Regeneration steam consumption, with good effects of energy saving and emission reduction.With use air as molten sulfur degasification bubbling source of the gas
Compare, change not oxygenous in mixed gas, on the premise of molten sulfur degasification effect is ensured, it is to avoid to sulphur
Retracting device combustion furnace air distribution than influence, reduce sulfur recovery facility fluctuation make its even running, favorably
In reducing energy consumption.Compared with all employing nitrogen as bubbling source of the gas, it is possible to reduce nitrogen use level, work as utilization
When air-separating plant provides nitrogen, the load of air-separating plant can be significantly reduced, save electric energy.
In above-mentioned liquid sulphur degasification technique, the ratio of the nitrogen d and desulfidation tail gas m from desulfurizing tower is to de-
Gas effect and energy consumption have important influence.As described above, if desulfidation tail gas m in mixed gas e
Ratio is too high, can cause CO in molten sulfur degasification tail gas2Content is higher, increases follow-up net to molten sulfur degasification tail gas
Energy consumption during change；And if nitrogen d ratios are too high in mixed gas e, then can increase nitrogen use level,
Energy consumption can equally be increased.Therefore, the percent by volume of desulfidation tail gas m is 20%~60% in mixed gas e,
It is preferred that 30%~50%, for example can for 32%, 34%, 35%, 36%, 38%, 40%, 42%, 44%,
45%th, 46%, 48% etc., more preferably 35%~45%.
In above-mentioned liquid sulphur degasification technique, the no considered critical in source of nitrogen d comes preferably from air
The nitrogen of separator.Air-separating plant refer to by air liquefaction, rectifying, be finally recovered turn into oxygen,
The gas separation equipment of nitrogen and other valuable gases.
In above-mentioned liquid sulphur degasification technique, the molten sulfur degasification tail gas h produced by molten sulfur degasification can use with
Lower method carries out further purified treatment：Molten sulfur degasification tail gas h is delivered in hydrogenation reactor 8 first
Hydrogenation hydrolytic reaction is carried out under the conditions of 230 DEG C~240 DEG C, makes the organic sulfur compound in molten sulfur degasification tail gas, for example
COS、CS2Etc. being converted into H2S obtains hydrogenation tail gas k；Then hydrogenation tail gas k is delivered to desulfurizing tower 11
In carry out solution desulfurization and obtain desulfidation tail gas m；A part of desulfidation tail gas m is transmitted back to molten sulfur pond 1 and nitrogen again
Bubbling is carried out to molten sulfur after gas d mixing, remaining desulfidation tail gas are delivered into incinerator 15 is burned
Flue gas n, gained flue gas n is discharged by chimney 16.In above-mentioned solution sweetening process, the poor absorption of desulfurization
Temperature when liquid enters desulfurizing tower 11 is 30 DEG C~40 DEG C, and desulfuration solution internal circulating load is 70~85m3/ h, desulfurization
Solution regeneration steam consumption is 7.0~8.5t/h.Catalyst and solution used in the process of hydrogenation hydrolytic reaction
The specific species of desulfuration solution used does not have strict restriction, this area conventional technical means in sweetening process
.Wherein, preferably selecting property of desulfuration solution desulfuration solution high, such as amine desulphurization solvent, are absorbing
H in hydrogenation tail gas2CO will not be absorbed during S2Deng other sour gas, to ensure H2The assimilation effect of S.
It will be appreciated by persons skilled in the art that hydrogenation reactor 8 used in above-mentioned decontamination process,
In above-mentioned liquid sulphur degasification technique, molten sulfur degasification tail gas h is delivered to hydrogenation instead using jet pump 6
Answer in device 8, the steam pressure of jet pump 6 is 500KPa~700KPa.Low-pressure fuel injection used by jet pump 6
Steam g can be the self-produced steam from sulfur recovery facility, should not thus use compressor or air inducing
Machine, had both been avoided that blocking of the sulphur to equipment, and the consumption of electric energy can be reduced again.
In above-mentioned liquid sulphur degasification technique, because the temperature in molten sulfur pond 1 is 140 DEG C~160 DEG C, and it is hydrogenated with
Reaction temperature in reactor 8 is 230 DEG C~240 DEG C, in order that molten sulfur degasification tail gas h enters hydrogenation reactor
Can quickly be reacted after 8, to reduce the energy consumption of hydrogenation reactor 8, be delivered to by molten sulfur degasification tail gas h
Before hydrogenation reactor 8, first it is transported to be preheated in online combustion furnace 7.
In above-mentioned liquid sulphur degasification technique, because the temperature in desulfurizing tower 11 is relatively low, therefore tail gas will be hydrogenated with
K is delivered to waste heat boiler 9 and carries out heat recovery, is then sent to after chilling tower 10 is cooled to 35 DEG C~45 DEG C
Being delivered to again in desulfurizing tower 11 carries out solution desulfurization.
It will be appreciated by persons skilled in the art that online combustion furnace 7 used in above-mentioned decontamination process,
Hydrogenation reactor 8, waste heat boiler 9, chilling tower 10 and desulfurizing tower 11 are directly using sulfur recovery facility
Exhaust gas purification equipment, it is not necessary to extra newly-built.The tail gas i of molten sulfur degasification tail gas h and sulfur recovery facility
Together subsequent purification treatment is carried out into online combustion furnace 7.
Come to make further specifically the liquid sulphur degasification technique of the embodiment of the present invention below by specific experiment data
It is bright.
Embodiment 1
The present embodiment provides a kind of liquid sulphur degasification technique, and referring to Fig. 1, the technique is comprised the following steps：
Step 1, by the nitrogen d from air-separating plant (not shown) and from desulfurizing tower 11
The mixed gas e of desulfidation tail gas m is passed through in molten sulfur pond 1, using bubbler 2 under the conditions of 140 DEG C to liquid
Sulphur a carries out bubbling, the sulfide in molten sulfur 1 is obtained the molten sulfur f and molten sulfur degasification tail gas h that deaerates into gas phase.
Wherein, the percent by volume of desulfidation tail gas m is 30% in mixed gas e, and the percent by volume of nitrogen d is
70%.The flow of nitrogen d is adjusted by nitrogen flow regulating valve 3 and nitrogen stream scale 4, by de-
Sulphur exhaust flow regulating valve 13 and desulfidation tail gas flowmeter 14 are adjusted to the flow of desulfidation tail gas m.It is de-
Gas-liquid sulphur f is delivered to upstream device by liquid sulfur pump 5, and the mass concentration of sulfide is in 10ppm in degassing molten sulfur f
Below.
, be delivered to molten sulfur degasification tail gas h in online combustion furnace 7 using jet pump 6 by step 2, and carrys out bin cure
The tail gas i of sulphur retracting device is preheated and is delivered to hydrogenation reactor 8 together carries out hydrogenation hydrolytic reaction, makes
Organic sulfur compound in tail gas is converted into H2S obtains hydrogenation tail gas k.Wherein, the steam pressure of jet pump 6 is
500KPa, the hydrogenation hydrolytic reaction in hydrogenation reactor 8 is carried out under the conditions of 230 DEG C.
Step 3, hydrogenation tail gas k is delivered into waste heat boiler 9 carries out heat recovery, is then sent to chilling tower
10 be cooled to 40 DEG C after be delivered to again in desulfurizing tower 11 and carry out solution desulfurization, obtain desulfidation tail gas m.Solution
In sweetening process, temperature when the poor absorbing liquid of desulfurization enters desulfurizing tower 11 is 30 DEG C, desulfuration solution internal circulating load
It is 70m3/ h, desulfuration solution regeneration steam consumption is 7.1t/h.
Step 4, molten sulfur pond 1 is transmitted back to by a part of desulfidation tail gas m by air-introduced machine 12, and from air
Bubbling is carried out to molten sulfur a after the nitrogen d mixing of separator, remaining desulfidation tail gas m is delivered to burning
Stove 15 burn and obtains flue gas n, is discharged flue gas n by chimney 16.
After testing, H in step 3 gained desulfidation tail gas in the present embodiment2The content of S is 15mg/m3, step 4
SO in gained flue gas2Content be 40mg/m3。
Embodiment 2
The present embodiment provides a kind of liquid sulphur degasification technique, and referring to Fig. 1, the technique is comprised the following steps：
Step 1, by the nitrogen d from air-separating plant (not shown) and from desulfurizing tower 11
The mixed gas e of desulfidation tail gas m is passed through in molten sulfur pond 1, using bubbler 2 under the conditions of 150 DEG C to liquid
Sulphur a carries out bubbling, the sulfide in molten sulfur 1 is obtained the molten sulfur f and molten sulfur degasification tail gas h that deaerates into gas phase.
Wherein, the percent by volume of desulfidation tail gas m is 40% in mixed gas e, and the percent by volume of nitrogen d is
60%.The flow of nitrogen d is adjusted by nitrogen flow regulating valve 3 and nitrogen stream scale 4, by de-
Sulphur exhaust flow regulating valve 13 and desulfidation tail gas flowmeter 14 are adjusted to the flow of desulfidation tail gas m.It is de-
Gas-liquid sulphur f is delivered to upstream device by liquid sulfur pump 5, and the mass concentration of sulfide is in 10ppm in degassing molten sulfur f
Below.
, be delivered to molten sulfur degasification tail gas h in online combustion furnace 7 using jet pump 6 by step 2, and carrys out bin cure
The tail gas i of sulphur retracting device is preheated and is delivered to hydrogenation reactor 8 together carries out hydrogenation hydrolytic reaction, makes
Organic sulfur compound in tail gas is converted into H2S obtains hydrogenation tail gas k.Wherein, the steam pressure of jet pump 6 is
600KPa, the hydrogenation hydrolytic reaction in hydrogenation reactor 8 is carried out under the conditions of 235 DEG C.
Step 3, hydrogenation tail gas k is delivered into waste heat boiler 9 carries out heat recovery, is then sent to chilling tower
10 be cooled to 40 DEG C after be delivered to again in desulfurizing tower 11 and carry out solution desulfurization, obtain desulfidation tail gas m.Solution
In sweetening process, temperature when the poor absorbing liquid of desulfurization enters desulfurizing tower 11 is 30 DEG C, desulfuration solution internal circulating load
It is 76m3/ h, desulfuration solution regeneration steam consumption is 7.5t/h.
Step 4, molten sulfur pond 1 is transmitted back to by a part of desulfidation tail gas m by air-introduced machine 12, and from air
Bubbling is carried out to molten sulfur a after the nitrogen d mixing of separator, remaining desulfidation tail gas m is delivered to burning
Stove 15 burn and obtains flue gas n, is discharged flue gas n by chimney 16.
After testing, H in step 3 gained desulfidation tail gas in the present embodiment2The content of S is 23mg/m3, step 4
SO in gained flue gas2Content be 52mg/m3。
Embodiment 3
The present embodiment provides a kind of liquid sulphur degasification technique, and referring to Fig. 1, the technique is comprised the following steps：
Step 1, by the nitrogen d from air-separating plant (not shown) and from desulfurizing tower 11
The mixed gas e of desulfidation tail gas m is passed through in molten sulfur pond 1, using bubbler 2 under the conditions of 160 DEG C to liquid
Sulphur a carries out bubbling, the sulfide in molten sulfur 1 is obtained the molten sulfur f and molten sulfur degasification tail gas h that deaerates into gas phase.
Wherein, the percent by volume of desulfidation tail gas m is 50% in mixed gas e, and the percent by volume of nitrogen d is
50%.The flow of nitrogen d is adjusted by nitrogen flow regulating valve 3 and nitrogen stream scale 4, by de-
Sulphur exhaust flow regulating valve 13 and desulfidation tail gas flowmeter 14 are adjusted to the flow of desulfidation tail gas m.It is de-
Gas-liquid sulphur f is delivered to upstream device by liquid sulfur pump 5, and the mass concentration of sulfide is in 10ppm in degassing molten sulfur f
Below.
, be delivered to molten sulfur degasification tail gas h in online combustion furnace 7 using jet pump 6 by step 2, and carrys out bin cure
The tail gas i of sulphur retracting device is preheated and is delivered to hydrogenation reactor 8 together carries out hydrogenation hydrolytic reaction, makes
Organic sulfur compound in tail gas is converted into H2S obtains hydrogenation tail gas k.Wherein, the steam pressure of jet pump 6 is
700KPa, the hydrogenation hydrolytic reaction in hydrogenation reactor 8 is carried out under the conditions of 240 DEG C.
Step 3, hydrogenation tail gas k is delivered into waste heat boiler 9 carries out heat recovery, is then sent to chilling tower
10 be cooled to 40 DEG C after be delivered to again in desulfurizing tower 11 and carry out solution desulfurization, obtain desulfidation tail gas m.Solution
In sweetening process, temperature when the poor absorbing liquid of desulfurization enters desulfurizing tower 11 is 30 DEG C, desulfuration solution internal circulating load
It is 84m3/ h, desulfuration solution regeneration steam consumption is 8.3t/h.
Step 4, molten sulfur pond 1 is transmitted back to by a part of desulfidation tail gas m by air-introduced machine 12, and from air
Bubbling is carried out to molten sulfur a after the nitrogen d mixing of separator, remaining desulfidation tail gas m is delivered to burning
Stove 15 burn and obtains flue gas n, is discharged flue gas n by chimney 16.
After testing, H in step 3 gained desulfidation tail gas in the present embodiment2The content of S is 36mg/m3, step 4
SO in gained flue gas2Content be 71mg/m3。
Comparative example 1
This comparative example provides a kind of liquid sulphur degasification technique, and this comparative example is with the difference of embodiment 1, step 1
In bubbling is carried out to molten sulfur a only with the desulfidation tail gas m from desulfurizing tower 11, desulfuration solution is followed in step 3
Circular rector is 100m3/ h, desulfuration solution regeneration steam consumption is 8.8t/h.
After testing, H in desulfidation tail gas in this comparative example2The content of S is 92mg/m3, SO in flue gas2Contain
It is 130mg/m to measure3。
To sum up, sulfide in molten sulfur and right is removed using liquid sulphur degasification technique provided in an embodiment of the present invention
Molten sulfur degasification tail gas is processed, and can not only effectively remove the sulfide in molten sulfur, makes the vulcanization in molten sulfur
Thing content reaches below 10ppm, additionally it is possible to significantly reduce desulfuration solution in solution sweetening process internal circulating load and
Desulfuration solution regeneration steam consumption, compared with existing liquid sulphur degasification technique, desulfurization is molten in solution sweetening process
The internal circulating load of liquid reduces by more than 16%, regeneration energy consumption reduction by more than 5.7%, SO in the flue gas of final discharge2Contain
Amount is in 80mg/m3Below.
The above is for only for ease of it will be understood by those skilled in the art that technical scheme, and without
To limit the present invention.All any modifications within the spirit and principles in the present invention, made, equivalent,
Improve etc., should be included within the scope of the present invention.
Claims (9)
1. a kind of liquid sulphur degasification technique, it is characterised in that the liquid sulphur degasification technique includes：
The mixed gas of nitrogen and the desulfidation tail gas from desulfurizing tower are passed through in molten sulfur pond, at 140 DEG C~160 DEG C
Under the conditions of bubbling is carried out to molten sulfur, sulfide in molten sulfur is obtained deaerate molten sulfur and molten sulfur degasification into gas phase
Tail gas；The percent by volume of the desulfidation tail gas from desulfurizing tower described in the mixed gas is 20%~60%.
2. liquid sulphur degasification technique according to claim 1, it is characterised in that institute in the mixed gas
The percent by volume for stating the desulfidation tail gas from desulfurizing tower is 30%~50%.
3. liquid sulphur degasification technique according to claim 2, it is characterised in that institute in the mixed gas
The percent by volume for stating the desulfidation tail gas from desulfurizing tower is 35%~45%.
4. liquid sulphur degasification technique according to claim 1, it is characterised in that the nitrogen comes from air
Separator.
5. liquid sulphur degasification technique according to claim 1, it is characterised in that the liquid sulphur degasification technique
Also include：
The molten sulfur degasification tail gas is delivered in hydrogenation reactor and is hydrogenated with the conditions of 230 DEG C~240 DEG C
Hydrolysis, makes the organic sulfur compound in the molten sulfur degasification tail gas be converted into H2S obtains being hydrogenated with tail gas；
The hydrogenation tail gas is delivered to carry out solution desulfurization and obtains the desulfidation tail gas in the desulfurizing tower；Institute
State in solution sweetening process, temperature when the poor absorbing liquid of desulfurization enters the desulfurizing tower is 30 DEG C~40 DEG C；
A part of desulfidation tail gas are delivered to the molten sulfur pond, desulfidation tail gas described in another part are conveyed
To incinerator burn and obtain flue gas, and by the fume emission.
6. liquid sulphur degasification technique according to claim 5, it is characterised in that will be described using jet pump
Molten sulfur degasification tail gas is delivered in hydrogenation reactor, and the steam pressure of the jet pump is 500KPa~700KPa.
7. liquid sulphur degasification technique according to claim 5, it is characterised in that by the molten sulfur degasification tail
Gas is delivered to and is delivered to again in the hydrogenation reactor after line combustion furnace.
8. liquid sulphur degasification technique according to claim 5, it is characterised in that the hydrogenation tail gas is defeated
Delivering to waste heat boiler carries out heat recovery, then to be delivered to chilling tower cooler described de- to being delivered to after 35 DEG C~45 DEG C
Solution desulfurization is carried out in sulphur tower.
9. liquid sulphur degasification technique according to claim 5, it is characterised in that the solution sweetening process
In, desulfuration solution internal circulating load is 70~85m3/ h, desulfuration solution regeneration steam consumption is 7.0~8.5t/h.
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