CN109810740A - One kind being used for sulfur-containing gas Development & Multipurpose use system and technique - Google Patents
One kind being used for sulfur-containing gas Development & Multipurpose use system and technique Download PDFInfo
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 52
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 47
- 239000011593 sulfur Substances 0.000 title claims abstract description 47
- 239000007789 gas Substances 0.000 claims abstract description 234
- 239000002253 acid Substances 0.000 claims abstract description 107
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 101
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 54
- 230000023556 desulfurization Effects 0.000 claims abstract description 54
- 239000003345 natural gas Substances 0.000 claims abstract description 49
- 239000002918 waste heat Substances 0.000 claims abstract description 33
- 238000005262 decarbonization Methods 0.000 claims abstract description 14
- 150000001412 amines Chemical class 0.000 claims abstract description 13
- 238000000746 purification Methods 0.000 claims abstract description 10
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 263
- 239000007788 liquid Substances 0.000 claims description 91
- 239000000243 solution Substances 0.000 claims description 74
- 238000009833 condensation Methods 0.000 claims description 61
- 230000005494 condensation Effects 0.000 claims description 61
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 55
- 238000001816 cooling Methods 0.000 claims description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 44
- 238000010521 absorption reaction Methods 0.000 claims description 36
- 239000003949 liquefied natural gas Substances 0.000 claims description 32
- 238000004064 recycling Methods 0.000 claims description 31
- 238000003860 storage Methods 0.000 claims description 24
- 239000012535 impurity Substances 0.000 claims description 21
- 239000003595 mist Substances 0.000 claims description 21
- 239000000203 mixture Substances 0.000 claims description 17
- 239000003507 refrigerant Substances 0.000 claims description 16
- 239000003054 catalyst Substances 0.000 claims description 14
- 238000002485 combustion reaction Methods 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 12
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 11
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 11
- 230000005484 gravity Effects 0.000 claims description 11
- 239000004571 lime Substances 0.000 claims description 11
- 229930195733 hydrocarbon Natural products 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 10
- 238000010926 purge Methods 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 9
- 238000006703 hydration reaction Methods 0.000 claims description 9
- 150000002430 hydrocarbons Chemical class 0.000 claims description 9
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 claims description 8
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims description 8
- 239000012141 concentrate Substances 0.000 claims description 8
- 239000010410 layer Substances 0.000 claims description 8
- 238000004090 dissolution Methods 0.000 claims description 7
- 239000002737 fuel gas Substances 0.000 claims description 7
- 239000007864 aqueous solution Substances 0.000 claims description 6
- 238000007701 flash-distillation Methods 0.000 claims description 6
- 230000005611 electricity Effects 0.000 claims description 5
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 238000010792 warming Methods 0.000 claims description 4
- 230000001112 coagulating effect Effects 0.000 claims description 3
- 239000011229 interlayer Substances 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 230000001133 acceleration Effects 0.000 claims 1
- 238000000926 separation method Methods 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 4
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 230000006978 adaptation Effects 0.000 abstract 1
- 238000000605 extraction Methods 0.000 abstract 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 31
- 229910002092 carbon dioxide Inorganic materials 0.000 description 26
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 19
- 230000018109 developmental process Effects 0.000 description 11
- 239000005864 Sulphur Substances 0.000 description 6
- 238000011084 recovery Methods 0.000 description 6
- 238000010276 construction Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 230000002378 acidificating effect Effects 0.000 description 3
- 239000000110 cooling liquid Substances 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000000536 complexating effect Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- PCHPORCSPXIHLZ-UHFFFAOYSA-N diphenhydramine hydrochloride Chemical compound [Cl-].C=1C=CC=CC=1C(OCC[NH+](C)C)C1=CC=CC=C1 PCHPORCSPXIHLZ-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 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
- 239000012071 phase Substances 0.000 description 2
- QZAYGJVTTNCVMB-UHFFFAOYSA-N serotonin Chemical compound C1=C(O)C=C2C(CCN)=CNC2=C1 QZAYGJVTTNCVMB-UHFFFAOYSA-N 0.000 description 2
- LRDIEHDJWYRVPT-UHFFFAOYSA-N 4-amino-5-hydroxynaphthalene-1-sulfonic acid Chemical compound C1=CC(O)=C2C(N)=CC=C(S(O)(=O)=O)C2=C1 LRDIEHDJWYRVPT-UHFFFAOYSA-N 0.000 description 1
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N dimethylmethane Natural products CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
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- 238000001704 evaporation Methods 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
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- 238000002844 melting Methods 0.000 description 1
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- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- -1 propane Hydrocarbon Chemical class 0.000 description 1
- 230000007115 recruitment Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 210000000582 semen Anatomy 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 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
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- 230000008016 vaporization Effects 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention belongs to natural gas processing and applied technical fields, and in particular to one kind is used for sulfur-containing gas Development & Multipurpose use system and technique.One kind being used for sulfur-containing gas Development & Multipurpose use system, including amine desulfurization decarbonization system, wet process acid making system, afterheat generating system and LNG liquefaction system.The present invention solves the problems such as generating waste water, waste residue, exhaust gas in sulfur-containing gas exploitation purification and deep-processing process, waste heat boiler cogeneration is utilized simultaneously, system operation cost is greatly reduced, security risk is reduced, has prevented the problems such as environmental pollution, it is short with process flow, acid gas concentration wide adaptation range, the national environmental standard that exhaust emissions after final process fully meets and is suitable for being increasingly stringenter in the future, the strategic objective for really realizing Enterprise Circular Economy, can be widely applied basic, normal, high, extra-high natural gas extraction and purification and field of deep.
Description
Technical field
The invention belongs to natural gas processing and applied technical fields, and in particular to one kind is for sulfur-containing gas exploitation synthesis
Utilize system and technique.
Background technique
Natural gas is naturally occurred in the void layer of underground, is based on the low molecules saturated hydrocarbons such as methane, ethane, propane
Hydrocarbon gas and the non-hydrocarbon gases composition such as a small amount of hydrogen sulfide, carbon dioxide, nitrogen mixed gas.It is as a kind of clear
Clean, efficient and good Gas Energy Source and industrial chemicals are widely used in gas, natural gas liquefaction, natural gas power and day
So multiple fields such as gasification work.As " sending in river gas east " pipeline and " the second west to east gas pipeline project " are completely gone into operation, China has been basically formed
National natural gas backbone pipe network.Under the requirement of national policy, under conditions of market demand is increasingly vigorous, China is just welcome
The natural gas of one wave " natural gas tide " from underground usually contains H2S、CO2Etc. components, H2S and CO2The presence of equal sour gas
It will cause the corrosion of pipeline, equipment etc., and accelerated corrosion under the conditions of having existing for water, it is therefore desirable to CO2It is separated, it is right
H2S is recycled, and the content of usual CO2 is less, and recovery value is not high, therefore only to H2S is recycled, the recycling work of hydrogen sulfide
Skill mainly has sulfur recovery and acid recovery, and based on claus process, Complexing Iron wet desulfurizing process also has sulfur recovery technology in succession
Application, but there are still problems, claus process investment is larger, takes up a large area, and the construction period is long, tail gas there are still
SO2Excessive problem, and Complexing Iron wet desulfurizing process problem is even more serious, desulfurization medicament internal circulating load is big, and it is low that there are sulfur purities
(only 70%), wet process sulphur technique sulphur refining stage generate a large amount of brine waste, it is more difficult to handle.
It is more and more stringent with environmental protection standard, need to develop the new exploitation of individual well sulfur-containing gas and deep process skill
Art, the new process and device for solving the station desulfurization of individual well well, reducing capital expenditure, reducing O&M cost, reduce environmental pollution.
Summary of the invention
It is an object of the invention to ask for present in existing sulfur-containing gas Well Development and deep process technology
Topic provides sulfur-containing gas Development & Multipurpose use system and technique, which is guaranteeing selexol process and natural gas deep processing
Under the premise of reduce energy consumption as far as possible, realize the recycling and resource utilization of sulphur, realize cogeneration recycling.
The technical scheme is that
One kind be used for sulfur-containing gas Development & Multipurpose use system, including amine desulfurization decarbonization system, wet process acid making system,
Afterheat generating system and LNG liquefaction system.
The amine desulfurization decarbonization system includes gravity separator, and gravity separator is connect with absorption tower,
Purified natural gas after the desulfurization that absorbing tower top row comes out enters purge gas separator, and purified gas separating device, which is isolated, takes liquid
With it is defeated outside the purified gas after impurity；The rich solution ejected from the tower bottom on absorption tower enters flash tank, flashes away dissolution through flash tank
Hydro carbons after gas from flash drum overhead outlet be discharged into wet process acid making system；Rich solution after flash tank flashes passed through
Filter enters lean/rich liquid heat exchanger after filtering out impurity, and the outlet of lean/rich liquid heat exchanger is connect with regenerator；Regenerator tower bottom
Outlet is connect with reboiler, further removes H through reboiler2S and CO2, remove H2S and CO2Lean solution from reboiler be discharged by poor
It is cooling to enter poor rich liquid heat exchanger after liquid pump pressurization, is pumped into absorption tower by doctor solution circulation after poor rich liquid heat exchanger is cooling
Circulation desulfurization；The gas of regeneration column overhead discharge enters the cooling recycling lean solution of acid gas cooler, poor after acid gas cooler is cooling
Liquid enters return tank, and reflux pot bottom is connect with regenerator, and discharge gas enters wet process acid making system at the top of the return tank.
The wet process acid making system includes acid gas incinerator, and the flash drum overhead outlet connects with acid gas incinerator
It connects, the acid gas incinerator gas discharge outlet and SO2Converter connection, the SO2Converter is connect with condensation of sulfuric acid device,
Condensation of sulfuric acid device bottom discharge outlet connects heat exchanger, and heat exchanger outlet is connected to sulfuric acid storage tank, the sulfuric acid storage tank discharge
Sulfuric acid by sulfuric acid pump and sulfuric acid circulating pump outlet；The gas being discharged at the top of the condensation of sulfuric acid device is entered by gas discharge outlet
In acid mist eliminator, the sulfuric acid in sulfuric acid storage tank is sprayed into acid mist eliminator inner top by sulfuric acid circulating pump, and on-condensible gas is from acid mist
Chimney at the top of trap is discharged into atmosphere.
The afterheat generating system includes waste heat boiler, the top gas outlet and waste heat of the acid gas incinerator
Boiler connection, the SO2The top gas outlet of converter is connect with waste heat boiler, the waste heat boiler top vent
Mouth is connected to solidifying gas steam turbine, and generator is arranged at the solidifying gas steam turbine；The solidifying gas steam turbine bottom liquid discharge
The lime set water tank of mouth setting recycling condensed water, the condensed water of the recycling are pressurized after the discharge of lime set water tank by condensate pump laggard
Enter heat exchanger, heat exchanger is connect with reboiler.
The LNG liquefaction system include desulfurization pretreatment device, several grades of heat exchangers and be mounted on heat exchangers at different levels into
Several gas-liquid separators at mouthful, the purified gas that purified gas separating device isolates after taking liquid and impurity enter desulfurization pretreatment dress
Set, enter first-class heat exchanger through the processed purification gas of desulfurization pretreatment device, mix refrigerant successively pass through compressor one,
Enter in first-class heat exchanger after water cooler and gas-liquid separator one, by first-class heat exchanger gaseous state mix refrigerant after cooling
Into gas-liquid separator two, secondary heat exchanger is respectively enterd by first-class heat exchanger liquid phase after cooling, by secondary heat exchange
Device gaseous state mix refrigerant after cooling enters gas-liquid separator three, respectively enters by secondary heat exchanger liquid phase after cooling
Three-level heat exchanger, out of the whole grade gas-liquid separator of liquid phase process of afterbody heat exchanger out, whole grade gas-liquid separator
Not solidifying natural gas is liquefied again into first-class heat exchanger either into acid gas incinerator as fuel gas after entering compressor two
It uses, the liquefied natural gas in whole grade gas-liquid separator enters storage in LNG storage tank.
Specifically, lean solution cooler is arranged between the poor rich liquid heat exchanger and doctor solution circulating pump.
Specifically, reflux pump is arranged between the return tank and regenerator.
Specifically, the heat exchanger includes heat exchanger one and heat exchanger two.
Specifically, setting is blown into the air blower of fresh air at the heat exchanger two, the heat exchanger two with it is described
Condensation of sulfuric acid device at the top of connection, the condensation of sulfuric acid device bottom discharge liquor enters acid gas incinerator.
Specifically, the SO2Converter is vertical vessel, inside sets three layers of catalyst bed, under every layer of catalyst bed
Side is respectively equipped with interlayer cooling device.
Use the work as described above that natural gas processing and application are carried out for sulfur-containing gas Development & Multipurpose use system
Skill includes the following steps: step 1: sulfur-containing gas first passes through gravity separator and removes the drop and solid wherein carried secretly
Impurity enters back into the absorbing liquid counter current contacting in absorption tower and tower, removes H2S and CO2, after the desulfurization that absorbing tower top row comes out
Purified natural gas isolated after the purge gas separator of outlet take it is defeated outside liquid and impurity after-purification gas；Go out from absorbing tower bottom
Come richness it is molten, first pass through flash tank flash away dissolution hydro carbons enter acid gas incinerator oxygen-excess combustion generate SO2；Step 2: warp
Rich solution after flash tank flash distillation enters after lean/rich liquid heat exchanger is warming up to 105 DEG C after filter filters out impurity and enters again
Raw tower, rich solution contact with upstream high-temperature steam in regenerator and desorb H2S and CO2；Regenerator tower bottom come out 120
DEG C semi lean solution enters reboiler and further removes H2S and CO2, remove H2S and CO2Lean solution be pressurized by lean pump after through lean/rich liquid
After heat exchanger is cooling, then through lean solution cooler is cold cool down again after by doctor solution circulation be pumped into absorption tower circulation desulfurization；From
The acid gas that regenerator desorbs enters the cooling recycling lean solution of acid gas cooler, and lean solution enters return tank by return tank bottom after cooling
The reflux pump of portion's setting is delivered to regenerator and carries out recycling and reusing；Step 3: the concentrate sour gas being discharged at the top of return tank
Into acid gas incinerator, sour gas carries out oxygen-excess combustion in acid gas incinerator and generates SO2, SO in acid gas incinerator2Gas
Enter SO after waste heat boiler crosses the heat exchange cooling of furnace2Converter, in SO2SO in converter2It is converted under the action of catalyst
SO3；Step 4: after temperature is down to sulfuric acid vapor dew point, SO3Gas enters condensation of sulfuric acid device, SO in condensation of sulfuric acid device3Gas
It is flowed up in tube side with water vapour and hydration reaction generation H occurs2SO4, and as the reduction of temperature is condensed into mass fraction
98% liquid heat sulfuric acid, hot sulfuric acid temperature is 246 DEG C or so, using heat exchanger two after heat exchanger one drops to 150 DEG C
Heat exchange be cooled to 40 DEG C or so it is rear enter sulfuric acid storage tank, it is then periodically outer defeated by sulfuric acid pump entrucking；Step 5: condensation of sulfuric acid device top
The gas of portion's discharge enters acid mist eliminator, and the cold sulfuric acid that gas and sulfuric acid circulating pump are sprayed into from top in acid mist eliminator is inverse
Stream contact, realizes the condensation recycling of sulfuric acid vapor, and on-condensible gas is discharged into atmosphere from chimney；Step 6: air blower blasts new
Fresh air first passes around heat exchanger two and is cooled down again to 150 DEG C of the sulfuric acid from heat exchanger one, cold subsequently into sulfuric acid
Condenser top and condensation of sulfuric acid device lower part come from SO2The SO of converter3Heat exchange, which is carried out, with vapor realizes SO3With vapor
Hydration reaction, the concentrate acid gas that acid gas incinerator and the discharge of return tank top are then entered after the discharge of condensation of sulfuric acid device bottom are sent out
Raw oxygen-excess combustion reaction, realizes H2S is converted into SO2；Step 7: more than the middle super pressure-high temperature steam entrance be discharged by waste heat boiler top
The solidifying gas steam turbine of heat generating system, is generated electricity by generator, hot steam is pressed through in realization by thermal energy and is converted into electric energy；Middle pressure
High-temperature steam temperature after coagulating gas steam turbine drops to 100 DEG C hereinafter, realizing the condensation of steam, and steam enters the realization of lime set water tank
The recycling of condensed water, the condensed water of recycling enter heat exchanger one after being pressurized by condensate pump, then enter sulfuric acid by heat exchanger one
Condenser cools down to the hot sulfuric acid in condensation of sulfuric acid device；It is de- to enter amine method after the condensed water heating in heat exchanger one simultaneously
The reboiler of sulphur decarbonization system accelerates the sour gas solution dissolved and absorbed in semi lean solution for the heating to semi lean solution in reboiler
It inhales, the condensed water in reboiler is through SO2Converter enters waste heat boiler and recycles；Step 8: it is come out from purge gas separator
Purified natural gas enter desulfurization pretreatment device, be dehydrated in desulfurization pretreatment device, desulfurization, demercuration, after pretreatment
Purified natural gas enter several grades of heat exchangers of LNG liquefaction system after cool down, then go out by whole grade gas-liquid separator separates
Enter LNG storage tank after not solidifying natural gas and formed defeated outside finished product LNG, not solidifying natural gas enters acid gas after compressor boost and burns
Furnace uses as fuel gas or enters the first-class heat exchanger entrance of LNG liquefaction system to be liquefied again.
Specifically, the absorbing liquid in the absorption tower is the aqueous solution that concentration is 40~45%MDEA, absorption tower internal pressure
Power is 3.5~4.0Mpa.
Specifically, the SO2Catalyst in reactor is V2O5。
Specifically, the temperature for the middle super pressure-high temperature steam being discharged at the top of the waste heat boiler is 420 DEG C, pressure is
3.9Mpa。
The system integration provided by the invention sulfur-containing gas desulfurization and decarburization, sour gas (H2S) relieving haperacidity (H2SO4), purification day
The systems such as right gas LNG, cogeneration, the construction of sulfur-containing gas low cost development, low cost operation, natural gas liquefaction store,
It responds national energy and comprehensively utilizes strategic, while Various Seasonal can be realized to the peak regulation demand of combustion gas.The present invention also has
Following characteristics: 1. sulfur recovery rate is high, and the rate of recovery of sulphur is up to 99.9% or more；2. being applicable in sulfur-containing gas flow, sulfur content etc.
Fluctuation range is wide, can handle H2Sour gas of the S volume fraction in 3%~60% range；3. non-environmental-pollution, technique letter
List does not have chemicals consumption and sewage discharge, and the thermal efficiency is high, finished product is high quality sulfuric acid (concentration 92~98%), not recruitment
Skill water, does not generate waste residue or waste water, does not have secondary pollution to environment；4. operating cost is low, starting fluid is needed when driving except device
Needed outside external heat source when with thermal medium-molten salt melting, once get into smooth, can high efficiente callback a large amount of technological reaction heat, by-product
4.0MPa, 420 DEG C of superheated steam, are used for cogeneration, and reuse drives electrical equipment；5. high degree of automation, whole set process
It is automatically controlled using DCS.Sulfur-containing gas Development & Multipurpose use technique and system provided by the present invention greatly reduce construction
Cost of investment；Shorten the construction period；Waste water, waste residue are not generated in operational process；The income from sales of purified natural gas is improved,
It realizes that waste heat recycles simultaneously, can be widely applied to sulfur-containing gas exploitation and deep processing.
Detailed description of the invention
Fig. 1 is structural schematic diagram of the invention.
Wherein arrow refers to gas or liquid flow direction.
1 gravity separator, 2 absorption towers, 3 clarifier separators, 4 flash tanks, 5 filters, 6 lean/rich liquid heat exchangers, 7 are again
Raw tower, 8 reboilers, 9 lean solution booster pumps, 10 doctor solution coolers, 11 doctor solution circulating pumps, 12 acid gas coolers, 13 return tanks,
14 reflux pumps, 15 acid gas incinerators, 16 waste heat boilers, 17SO2Converter, 18 condensation of sulfuric acid devices, 19 heat exchangers one, 20 heat exchangers
Two, 21 sulfuric acid storage tanks, 22 sulfuric acid pumps, 23 acid mist eliminators, 24 chimneys, 25 sulfuric acid circulating pumps, 26 air blowers, 27 solidifying gas steamers
Machine, 28 condensate tanks, 29 condensate pumps, 30 generators, 31LNG output pump, 32 desulfurization pretreatment devices, 33 compressors one, 34
Water cooler, 35 gas-liquid separators one, 36 first-class heat exchangers, 37 gas-liquid separators two, 38 secondary heat exchangers, 39 gas-liquid separators
Three, 40 three-level heat exchangers, 41 gas-liquid separators four, 42 level Four heat exchangers, 43 compressors two, 44 gas-liquid separators five, 45LNG storage
Tank.
Specific embodiment
It is as shown in Figure 1 a kind of structural schematic diagram for sulfur-containing gas Development & Multipurpose use system, which includes
Amine desulfurization decarbonization system, wet process acid making system, LNG liquefaction system and afterheat generating system.
The amine desulfurization decarbonization system includes gravity separator 1, and gravity separator 1 and absorption tower 2 connect
It connects, the purified natural gas after the desulfurization that 2 tower top of absorption tower ejects enters purge gas separator 3, and purified gas separating device 3 separates
It is defeated outside purified gas after taking liquid and impurity out；The rich solution ejected from the tower bottom on absorption tower 2 enters flash tank 4, dodges through flash tank 4
Gas after evaporating the hydro carbons of dissolution is discharged into wet process acid making system from 4 top exit of flash tank；After the flash distillation of flash tank 4
Rich solution enters lean/rich liquid heat exchanger 6 after filter 5 filters out impurity, and the outlet of lean/rich liquid heat exchanger 6 and regenerator 7 connect
It connects；The outlet of 7 tower bottom of regenerator is connect with reboiler 8, further removes H through reboiler 82S and CO2, remove H2S and CO2Lean solution
It is cooling to enter poor rich liquid heat exchanger 6 after being pressurized from the discharge of reboiler 8 by lean pump 9, by de- after poor rich liquid heat exchanger 6 is cooling
Sulphur liquid circulating pump 11 is sent into 2 circulation desulfurization of absorption tower, and it is cooling that lean solution is arranged between poor rich liquid heat exchanger 6 and doctor solution circulating pump 11
Device 10；The gas of 7 tower top of regenerator discharge enters the cooling recycling lean solution of acid gas cooler 12, poor after acid gas cooler 12 is cooling
Liquid enters return tank 13, and 13 bottom of return tank is connect with regenerator 7, and reflux pump 14, institute are arranged between return tank 13 and regenerator 7
Gas is discharged at the top of the return tank 13 stated and enters wet process acid making system.
The wet process acid making system includes acid gas incinerator 15,4 top exit of flash tank and acid gas incinerator
15 connections, 15 gas discharge outlet of acid gas incinerator and SO2Converter 17 connects, the SO2Converter 17 and sulfuric acid are cold
Condenser 18 connects, and 18 bottom discharge outlet of condensation of sulfuric acid device is sequentially connected heat exchanger 1 and heat exchanger 2 20,2 20 row of heat exchanger
Outlet is connected to sulfuric acid storage tank 21, and the sulfuric acid that the sulfuric acid storage tank 21 is discharged is by 25 outlet of sulfuric acid pump 22 and sulfuric acid circulating pump；
The gas being discharged at the top of the condensation of sulfuric acid device 18 is entered in acid mist eliminator 23 by gas discharge outlet, and sulfuric acid circulating pump 25 will
Sulfuric acid in sulfuric acid storage tank 21 sprays into 23 inner top of acid mist eliminator, chimney 24 row of the on-condensible gas from 23 top of acid mist eliminator
Enter in atmosphere；Setting is blown into the air blower 26 of fresh air at the heat exchanger 2 20, the heat exchanger 2 20 with it is described
Condensation of sulfuric acid device 18 at the top of connect, the 18 bottom discharge liquor of condensation of sulfuric acid device enters acid gas incinerator 15.
The afterheat generating system includes waste heat boiler 16, the top gas outlet of the acid gas incinerator 15 with
Waste heat boiler 16 connects, the SO2The top gas outlet of converter 17 is connect with waste heat boiler 16, the waste heat boiler
16 top vent of furnace is connected to solidifying gas steam turbine 27, and generator 30 is arranged at the solidifying gas steam turbine 27；The solidifying gas
The lime set water tank 28 of 27 bottom liquid outlet of steam turbine setting recycling condensed water, the condensed water of the recycling is through lime set water tank 28
Enter heat exchanger after being pressurized after discharge by condensate pump 29, heat exchanger is connect with reboiler 8.
The LNG liquefaction system includes desulfurization pretreatment device 32, several grades of heat exchangers and is mounted on heat exchangers at different levels
Several gas-liquid separators of entrance, purified gas separating device 3 isolates the purified gas after taking liquid and impurity and enters desulfurization to be located in advance
Device 32 is managed, enters first-class heat exchanger 36 through the processed purification gas of desulfurization pretreatment device 32, mix refrigerant successively passes through
Enter in first-class heat exchanger 36 after overcompression machine 1, water cooler 34 and gas-liquid separator 1, by first-class heat exchanger 36
Gaseous state mix refrigerant after cooling enters gas-liquid separator 2 37, by the liquid phase after cooling of first-class heat exchanger 36 respectively into
Enter secondary heat exchanger 38, enter gas-liquid separator 3 39 by the gaseous state mix refrigerant after cooling of secondary heat exchanger 38, passes through
The liquid phase after cooling of secondary heat exchanger 38 respectively enters three-level heat exchanger 40, the liquid phase warp come out from afterbody heat exchanger
Whole grade gas-liquid separator 44 is crossed, the not solidifying natural gas in whole grade gas-liquid separator 44 enters level-one heat exchange after entering compressor 2 43
Device 36 liquefies either use into acid gas incinerator 15 as fuel gas again, and the liquefaction in whole grade gas-liquid separator 44 is natural
Gas enters storage in LNG storage tank 45.
Use the work as described above that the construction of natural gas fields and application are carried out for sulfur-containing gas Development & Multipurpose use system
Skill includes the following steps: step 1: sulfur-containing gas first passes through gravity separator 1 and removes the drop wherein carried secretly and consolidate
Body impurity enters back into the absorbing liquid counter current contacting in absorption tower 2 and tower, removes H2S and CO2, desulfurization that 2 tower top of absorption tower ejects
Purified natural gas afterwards is isolated after the purge gas separator 3 by outlet takes liquid and impurity after-purification gas enters LNG liquefaction system
System；The richness come out from 2 tower bottom of absorption tower is molten, first passes through flash tank 4 and flashes away the hydro carbons of dissolution and enters 15 peroxide of acid gas incinerator
Burning generates SO2；Step 2: the rich solution after the flash distillation of flash tank 4 enters lean/rich liquid after filter 5 filters out impurity and changes
Hot device 6 enters regenerator 7 after being warming up to 105 DEG C, and rich solution is contacted with upstream high-temperature steam in regenerator 7 and desorbed
H2S and CO2；120 DEG C of semi lean solutions that 7 tower bottom of regenerator comes out enter the further removing H of reboiler 82S and CO2, remove H2S and CO2
Lean solution be pressurized by lean pump 9 after after lean/rich liquid heat exchanger 6 is cooling, then after lean solution cooler cold 10 cools down again by
Doctor solution circulating pump 11 is sent into 2 circulation desulfurization of absorption tower；It is cooling that the acid gas desorbed from regenerator 7 enters acid gas cooler 12
Recycle lean solution, it is cooling after lean solution enter the reflux pump 14 that return tank 13 is arranged by reflux pot bottom and be delivered to regenerator 7 and returned
It receives and recycles；Step 3: the concentrate sour gas being discharged at the top of return tank 13 enters acid gas incinerator 15, and sour gas is in acid gas
Oxygen-excess combustion is carried out in incinerator generates SO2, SO in acid gas incinerator 152Gas crosses the heat exchange cooling of furnace 16 by waste heat boiler
Enter SO afterwards2Converter 17, in SO2SO in converter 172In catalyst V2O5SO is converted under effect3；Step 4: when temperature drops
To sulfuric acid vapor dew point, SO3Gas enters condensation of sulfuric acid device 18, SO in condensation of sulfuric acid device 183Gas and water vapour are in tube side
It flows up and hydration reaction generation H occurs2SO4, and as the reduction of temperature is condensed into the liquid heat sulfuric acid of mass fraction 98%,
Hot sulfuric acid temperature is 246 DEG C or so, is cooled to 40 DEG C using the heat exchange of heat exchanger 2 20 after heat exchanger 1 drops to 150 DEG C
Enter sulfuric acid storage tank 21 behind left and right, it is then periodically outer defeated by 22 entrucking of sulfuric acid pump；Step 5: it is discharged at the top of condensation of sulfuric acid device 18
Gas enters acid mist eliminator 23, the cold sulfuric acid adverse current that gas and sulfuric acid circulating pump 25 are sprayed into from top in acid mist eliminator 23
Contact, realizes the condensation recycling of sulfuric acid vapor, and on-condensible gas is discharged into atmosphere from chimney 24；Step 6: what air blower 26 blasted
Fresh air first passes around 2 20 pairs of heat exchanger 150 DEG C of the sulfuric acid from heat exchanger 1 and is cooled down again, subsequently into
18 top of condensation of sulfuric acid device and 18 lower part of condensation of sulfuric acid device come from SO2The SO of converter 173Heat exchange realization is carried out with vapor
SO3With the hydration reaction of vapor, then enter on acid gas incinerator and return tank 13 after the discharge of 18 bottom of condensation of sulfuric acid device
Oxygen-excess combustion reaction occurs for the concentrate acid gas of portion's discharge, realizes H2S is converted into SO2；Step 7: by being discharged at the top of waste heat boiler 16
Middle super pressure-high temperature steam enter the solidifying gas steam turbine 27 of afterheat generating system, generated electricity by generator 29, heat pressed through in realization
Steam is converted into electric energy by thermal energy；Middle super pressure-high temperature steam temperature after solidifying gas steam turbine 27 drops to 100 DEG C hereinafter, realizing steam
Condensation, steam enters the recycling that lime set water tank 28 realizes condensed water, and the condensed water of recycling enters after being pressurized by condensate pump 29
Then heat exchanger 1 enters condensation of sulfuric acid device 18 by heat exchanger 1, cools down to the hot sulfuric acid in condensation of sulfuric acid device 18；
The reboiler 8 for entering amine desulfurization decarbonization system after the condensed water heating in heat exchanger 1 simultaneously is used for in reboiler 8 half
The heating of lean solution accelerates the sour gas dissolved and absorbed in semi lean solution desorption, and the condensed water in reboiler 8 is through SO2Converter 17
It is recycled into waste heat boiler 16；Step 8: the purified natural gas come out from purge gas separator 3 enters desulfurization pretreatment dress
14 are set, is dehydrated in desulfurization pretreatment device 14, desulfurization, demercuration, pretreated purified natural gas enters LNG liquefaction system
Cool down after several grades of heat exchangers of system, then enters LNG after the natural gas that whole grade gas-liquid separator 44 cannot not isolated solidifyingly and store up
Defeated outside the formation of tank 45 finished product LNG, not solidifying natural gas enters acid gas incinerator 15 as fuel gas after the pressurization of compressor 43 and uses
Or it is liquefied again into the first-class heat exchanger entrance of LNG liquefaction system.
Absorbing liquid in the absorption tower 2 is the aqueous solution that concentration is 40~45%MDEA, and pressure is in absorption tower 2
3.5~4.0Mpa, the SO2Catalyst in reactor 17 is V2O5, the middle pressure being discharged at the top of the waste heat boiler 16 is high
The temperature of warm steam is 420 DEG C, pressure 3.9Mpa.
The present invention carries out hydramine method using amine desulfurization decarbonization system and removes sour gas (CO2、H2S) technique uses MDEA
The aqueous solution of (40~45%) as absorption solution of acid gases, sour gas under pressurization and normal temperature condition, MDEA (40~
45%) aqueous solution absorbs the acidic components in natural gas in absorption tower 2 (3.5~4.0MPa), under the effect of the pressure into
Enter flash tank 4, due to the effect of instant decompression, the hydro carbons that makes to dissolve in rich solution and carry secretly is flashed off, and flashed vapour may be used as
The combustion-supporting gas of acid gas incinerator, rich solution after flash distillation enter lean/rich liquid heat exchanger 6 through filter 5, and regenerated hot alcohol are completed
Amine aqueous solution (abbreviation lean solution) exchanges heat and is preheated, subsequently into 7 top of regenerator operated under low pressure, in (the behaviour of regenerator 7
Make 50~60KPa of pressure, 80~85 DEG C of operation temperature tower top, 105~110 DEG C of tower bottom) in, rich solution goes out portion in flash overhead first
Divide acidic components, then flow from above to below, is contacted with the gas (most of is vapor) for heating vaporization in reboiler 8,
Remaining acidic components in solution are further stripped off, the hot lean solution for leaving reboiler 8 is recycled through lean/rich liquid heat exchanger 6
After heat, then proper temperature (40~45 DEG C) is cooled further to through doctor solution cooler 10 and is then pumped to by doctor solution circulation
2 top of absorption tower, completes to recycle.
Carrying out wet process acid-making process using wet process acid making system in the present invention is by H2Liquid sulfuric acid is made in S, by hydramine method
Sour gas (the CO separated at the top of regenerator 7 in removing sour gas device2、H2S) enter acid gas incinerator 15, sour gas
(CO2、H2S) combustion air provided with combustion air blower 26 is burnt in acid gas incinerator 15, H2S and O2Reaction
Generate SO2, temperature is 1175 DEG C or so, reaction equation H2S+1.5O2=SO2+H2O, the process gas generated in acid gas incinerator 15
Body exchanges heat through waste heat boiler 16 (gas bag 3.6~4.0MPa of pressure, 390~410 DEG C of temperature) after coming out of the stove and cools down, and gas is cooled
To about 435~450 DEG C, it is directly entered SO2Converter 17.
In SO2In converter 17, SO2Under the catalysis of the catalyst, it is converted into SO3, reaction equation SO2+0.5O2=SO3.?
SO2SO contained in gas in converter 172It is converted on three layers of adiabatic catalytic bed, temperature is down to 270 DEG C of sulfuric acid vapor dew point
Enter condensation of sulfuric acid device 18 through control of acid fog device after above.Condensation of sulfuric acid device 18 is a falling-film condenser, by multiple groups parallel connection
Glass tube composition, glass tube be furnished with helix and demister.H contained in gas2SO4In condensation of sulfuric acid device 18 tube side to
Upper flowing, by the sulfuric acid after air setting along the acid mist eliminator 23 that glass tube walls flow to bottom；In condensation of sulfuric acid device 18
SO3With H2O hydration reaction generates gas phase H2SO4, reaction equation SO3+H2O=H2SO4；Then gas phase H2SO4It is condensed by air cooling-down
Sulfuric acid, gas walks tube side in condensation of sulfuric acid device 18, enters from bottom, cooling with air, condenses about 240 DEG C of generation, concentration
97% hot sulfuric acid, then mixed with SAPMAC method acid, mixed temperature is 60 DEG C, subsequently into acid mist eliminator 23, is cooled down
It is stored in sulfuric acid storage tank 21 to 40 DEG C of sulfate liquids, periodically by defeated outside tank car, 145 DEG C of tail gas of acid mist eliminator 23 reach
Discharge standard is discharged by chimney 24.
Embodiment 1
The present embodiment carries out the present invention and device detailed by taking certain sulfur-containing gas Well Development and comprehensive utilization as an example
It further illustrates.
15 × 104Nm3/d of certain sulfur-containing gas individual well natural gas production capacity；Sulfur-containing gas bleed pressure 5.0MPa,
Gas source temperature: 20 DEG C, component of natural gas is as shown in table 1 below.
Table 1: certain sulfur-containing gas gas well gas matter component table
Table 2: sulfur-containing gas LNG makings and product parameters table
The technique for carrying out desulfurization and application to the sulfur-containing gas individual well of certain sulfur-containing gas individual well natural gas is as follows:
It is 5.0MPa by pressure, the sulfur-containing gas that temperature is 20 DEG C (contains H2S 7.161%, CO25.512%) it first passes through
It crosses gravity separator 1 and removes the drop and solid impurity wherein carried secretly；Enter back into absorption tower 2 and its interior 40 DEG C MDEA liquid
Counter current contacting removes H2S and CO2.Purification of the purified natural gas by outlet after 43.3 DEG C of desulfurization that 2 tower top of absorption tower comes out
It is isolated after gas separating device 3 and takes liquid and impurity after-purification gas enters LNG liquefaction system and carries out liquefaction processing；From 2 tower bottom of absorption tower
The rich MDEA solution of 37.3 DEG C out, first passes through flash tank 4 and flashes away the hydro carbons of dissolution and enter acid gas incinerator 15 and carried out
Oxygen burning generates SO2；Rich solution MDEA after flash tank 4 flashes enters poor rich liquid heat exchanger 6 after filter 5 filters out impurity
Enter regenerator 7 after being warming up to 105 DEG C, is contacted with upstream high-temperature steam, desorb H2S and CO2.2 tower bottom of absorption tower goes out
The 120 DEG C of semi lean solutions come enter the further removing H of reboiler 82S and CO2, remove H2S and CO2Lean solution by lean pump 9 be pressurized after
After poor rich liquid heat exchanger 6 is cooled to 51 DEG C, then through lean solution cooler cold 10 but to being sent by doctor solution circulating pump 11 after 40 DEG C
Enter absorption tower circulation desulfurization, the acid gas (H desorbed2S、CO2) enter the cooling recycling lean solution of acid gas cooler 12, it is poor after cooling
Liquid enters the reflux pump 14 that return tank 13 is arranged by reflux pot bottom and is delivered to regenerator progress recycling and reusing.
The concentrate acid gas come out from 13 top of return tank enters wet H2The acid gas incinerator 15 of S acid making system, sour gas
(H2S oxygen-excess combustion) is carried out in acid gas incinerator generates SO2(2H2S+3O2→2SO2+2H2O), the SO of high temperature2(1200 DEG C of left sides
It is right) gas enters SO after being cooled to 435 DEG C or so after the heat exchange coil of waste heat boiler 162Converter 17, in SO2Converter
In 17, SO2In catalyst (V2O5) SO is converted under effect3(2SO2+O2→2SO3)。SO2Converter is vertical vessel, inside sets 3 layers
Catalyst bed, every layer of catalyst bed lower section are equipped with interlayer cooling device, to remove catalysis reaction heat, improve SO2To SO3
The conversion ratio of conversion.After temperature is down to sulfuric acid vapor dew point (280 DEG C or so) or more, SO2The SO generated in converter 173Into
Enter condensation of sulfuric acid device 18, SO in gas3Gas and water vapour flow up generation hydration reaction in 18 tube side of condensation of sulfuric acid device
Generate H2SO4, and as the reduction of temperature is condensed into the liquid heat sulfuric acid of about 246 DEG C, mass fraction 98%, hot sulfuric acid is by changing
Hot device 19, which exchanges heat after dropping to 150 DEG C using heat exchanger 20, is cooled to 40 DEG C or so rear entrance sulfuric acid storage tanks 21, then by sulfuric acid
It is periodically outer defeated to pump 22 entruckings.Gas (the sulfur-bearing sulfuric acid vapor, CO being discharged at the top of condensation of sulfuric acid device2、N2Deng) enter acid mist eliminator
23, the cold sulfuric acid counter current contacting sprayed into sulfuric acid circulating pump 25 from top in acid mist eliminator realizes the condensation of sulfuric acid vapor
Recycling, on-condensible gas (CO2、N2Deng) be discharged into atmosphere from chimney 24.It is right that the fresh air that air blower 26 blasts first passes around heat exchanger 20
150 DEG C of the sulfuric acid from heat exchanger 19 cools down, subsequently into 18 top of condensation of sulfuric acid device and 18 lower part of condensation of sulfuric acid device
From SO2The SO of converter 173Heat exchange, which is carried out, with vapor realizes SO3With the hydration reaction of vapor, then from condensation of sulfuric acid
Enter the concentrate acid of acid gas incinerator with 13 top of the return tank discharge from amine desulfurization decarbonization system after the discharge of 18 bottom of device
Oxygen-excess combustion reaction occurs for gas, realizes H2S is converted into SO2(2H2S+3O2→2SO2+2H2O)。
Middle super pressure-high temperature steam 3.9MPa, 420 DEG C of the superheated steam being discharged at the top of waste heat boiler 16 enter waste heat hair
The solidifying gas steam turbine 27 of electric system, generator 30 generate electricity, hot steam are pressed through in realization by thermal energy and is converted into electric energy；Overheat is steamed
Vapour temperature after coagulating gas steam turbine is reduced to 100 DEG C from 420 DEG C hereinafter, realizing the condensation of steam, and steam enters lime set water tank
28 realize the recycling of condensed water, and the condensed water of recycling is by entering heat exchanger 1 after the pressurization of condensate pump 29, then by heat exchanger
One 19 enter condensation of sulfuric acid device 18, cool down to the hot sulfuric acid in condensation of sulfuric acid device 18；Condensation in heat exchanger 1 simultaneously
Enter the reboiler 8 of amine desulfurization decarbonization system after water heating for the heating to semi lean solution in reboiler 8, accelerates in semi lean solution
The sour gas of solution absorption desorbs, and the condensed water in reboiler 8 is through SO2Converter 17 is recycled into waste heat boiler 16.
By entering the solidifying gas steam turbine 27 of afterheat generating system at the top of waste heat boiler 16, generated electricity by generator 29, in fact
Hot steam is pressed through in existing, and electric energy is converted by thermal energy；Middle super pressure-high temperature steam temperature after solidifying gas steam turbine 27 drop to 100 DEG C with
Under, realize the condensation of steam, steam enters the recycling that lime set water tank 28 realizes condensed water.
The purified natural gas come out from purge gas separator 3 enters desulfurization pretreatment device 14, in desulfurization pretreatment device
It is dehydrated in 14, desulfurization, demercuration, pretreated purified natural gas (pressure 4.6MPa, H2S content is less than 3.5mg/L, COS
Less than 0.1mg/L, CO2Content is less than 100mg/L, moisture content is less than 0.1mg/L, Hg content less than 0.01 μ g/m3) enter
The first-class heat exchanger 36 of LNG liquefaction system, mix refrigerant are compressed by compressor 1, after being water-cooled the cooling of device 34, into
Enter gas-liquid separator 1, purified natural gas and mix refrigerant respectively enter in first-class heat exchanger 36, and liquid exchanges heat in level-one
It throttles and cools down using throttle valve after being subcooled in device 36, mentioned jointly for first-class heat exchanger 36 after being mixed with the gas that backflows of subsequent process
Semen donors, cooled natural gas, gaseous state mix refrigerant and the liquid mixed refrigerant that need to be subcooled.Gaseous state mix refrigerant passes through one
Enter gas-liquid separator 2 37 after grade heat exchanger 36 is cooling, liquid phase respectively enters secondary heat exchanger 38, and liquid is subcooled and is saved
Secondary heat exchanger 38 being mixed into the gas that backflows after stream cooling, cooling capacity being provided, natural gas further cools down；Gaseous state mix refrigerant exists
It after being cooled in three-level heat exchanger 40, is subcooled in level Four heat exchanger 42, then returns to level Four after reducing pressure by regulating flow cooling and change
Hot device 42, with cooled natural gas and mix refrigerant；After purified natural gas flows successively through four heat exchangers, temperature is gradually decreased,
Then after the natural gas that whole grade gas-liquid separator 44 cannot not isolated solidifyingly enter LNG storage tank 45 formed finished product LNG (- 140 DEG C,
Defeated outside 3.9MPa), not solidifying natural gas enters acid gas incinerator 15 as fuel gas after the pressurization of compressor 43 and uses or enter LNG
36 entrance of first-class heat exchanger of liquefaction system is liquefied again.
The sulfur-containing gas Well Development and decarbonization desulfurization system, the total power consumption of Wet H2S acid making system in deep processing are about
1600kw/h, exportable 1600KW can satisfy the dynamic equipment of sulfur-containing gas individual well desulfurization and decarburization to afterheat generating system per hour
Whole power loads, every year can be with power cost saving 10013.76 ten thousand, while realizing 5,200,000 yuan of sulfuric acid income from sales.
Finally it should be noted that: the above embodiments are merely illustrative of the technical scheme of the present invention and are not intended to be limiting thereof；To the greatest extent
The present invention is described in detail with reference to preferred embodiments for pipe, it should be understood by those ordinary skilled in the art that: still
It can modify to a specific embodiment of the invention or some technical features can be equivalently replaced；Without departing from this hair
The spirit of bright technical solution should all cover within the scope of the technical scheme claimed by the invention.
Claims (10)
1. one kind is used for sulfur-containing gas Development & Multipurpose use system, including it is amine desulfurization decarbonization system, wet process acid making system, remaining
Heat generating system and LNG liquefaction system, which is characterized in that
The amine desulfurization decarbonization system includes gravity separator (1), gravity separator (1) and absorption tower (2)
Connection, the purified natural gas after the desulfurization that absorption tower (2) tower top ejects enter purge gas separator (3), purified gas separation
Device (3) isolates the purified gas after taking liquid and impurity and enters LNG liquefaction system；The rich solution ejected from the tower bottom of absorption tower (2)
Into flash tank (4), the gas after flash tank (4) flashes away the hydro carbons of dissolution is discharged into from flash tank (4) top exit
Wet process acid making system；Rich solution after flash tank (4) flash distillation enters lean/rich liquid after filter (5) filters out impurity and exchanges heat
The outlet of device (6), lean/rich liquid heat exchanger (6) is connect with regenerator (7)；The outlet of regenerator (7) tower bottom is connect with reboiler (8),
H is further removed through reboiler (8)2S and CO2, remove H2S and CO2Lean solution from reboiler (8) be discharged by lean pump (9) be pressurized
Enter poor rich liquid heat exchanger (6) cooling afterwards, is sent into and absorbs by doctor solution circulating pump (11) after poor rich liquid heat exchanger (6) are cooling
Tower (2) circulation desulfurization；The gas of regenerator (7) tower top discharge enters acid gas cooler (12) cooling recycling lean solution, cold through acid gas
But lean solution enters return tank (13) after device (12) is cooling, and return tank (13) bottom is connect with regenerator (7), the return tank
(13) discharge gas in top enters wet process acid making system；
The wet process acid making system includes acid gas incinerator (15), the flash tank (4) top exit and acid gas incinerator
(15) it connects, acid gas incinerator (15) gas discharge outlet and SO2Converter (17) connection, the SO2Converter (17)
It is connect with condensation of sulfuric acid device (18), condensation of sulfuric acid device (18) bottom discharge outlet connects heat exchanger, and heat exchanger outlet and sulfuric acid store up
Tank (21) connection, the sulfuric acid of the sulfuric acid storage tank (21) discharge is by sulfuric acid pump (22) and sulfuric acid circulating pump (25) outlet；It is described
Condensation of sulfuric acid device (18) at the top of the gas that is discharged entered in acid mist eliminator (23) by gas discharge outlet, sulfuric acid circulating pump (25)
Sulfuric acid in sulfuric acid storage tank (21) is sprayed into acid mist eliminator (23) inner top, on-condensible gas is at the top of acid mist eliminator (23)
Chimney (24) is discharged into atmosphere；
The afterheat generating system includes waste heat boiler (16), the top gas outlet of the acid gas incinerator (15) with
Waste heat boiler (16) connection, the SO2The top gas outlet of converter (17) is connect with waste heat boiler (16), described
Waste heat boiler (16) top vent is connected to solidifying gas steam turbine (27), and generator is arranged at the solidifying gas steam turbine (27)
(30)；The lime set water tank (28) of solidifying gas steam turbine (27) the bottom liquid outlet setting recycling condensed water, the recycling
Condensed water after lime set water tank (28) discharge by entering heat exchanger, heat exchanger and reboiler (8) after condensate pump (29) pressurization
Connection；
The LNG liquefaction system include desulfurization pretreatment device (32), several grades of heat exchangers and be mounted on heat exchangers at different levels into
Several gas-liquid separators at mouthful, purified gas separating device (3) isolates the purified gas after taking liquid and impurity and enters desulfurization to be located in advance
It manages device (32), enters first-class heat exchanger (36), mix refrigerant through desulfurization pretreatment device (32) processed purification gas
Successively enter in first-class heat exchanger (36) after compressor one (33), water cooler (34) and gas-liquid separator one (35), warp
It crosses first-class heat exchanger (36) gaseous state mix refrigerant after cooling and enters gas-liquid separator two (37), by first-class heat exchanger (36)
Liquid phase after cooling respectively enters secondary heat exchanger (38), by secondary heat exchanger (38) gaseous state mix refrigerant after cooling
Into gas-liquid separator three (39), three-level heat exchanger (40) are respectively enterd by secondary heat exchanger (38) liquid phase after cooling,
The liquid phase come out from afterbody heat exchanger passes through whole grade gas-liquid separator (44), not coagulating in whole grade gas-liquid separator (44)
Natural gas enters compressor two (43), and into first-class heat exchanger (36), liquefaction either enters acid gas incinerator (15) work again afterwards
It is used for fuel gas, the liquefied natural gas in whole grade gas-liquid separator (44) enters storage in LNG storage tank (45).
2. being used for sulfur-containing gas Development & Multipurpose use system according to claim 1, which is characterized in that the rich or poor liquid
Lean solution cooler (10) are set between heat exchanger (6) and doctor solution circulating pump (11).
3. being used for sulfur-containing gas Development & Multipurpose use system according to claim 1, which is characterized in that the return tank
(13) reflux pump (14) are set between regenerator (7).
4. being used for sulfur-containing gas Development & Multipurpose use system according to claim 1, which is characterized in that the heat exchanger
Including heat exchanger one (19) and heat exchanger two (20).
5. being used for sulfur-containing gas Development & Multipurpose use system according to claim 4, which is characterized in that the heat exchanger
Setting is blown into the air blower (26) of fresh air, the heat exchanger two (20) and the condensation of sulfuric acid device (18) at two (20)
Top connection, condensation of sulfuric acid device (18) bottom discharge liquor enter acid gas incinerator (15).
6. being used for sulfur-containing gas Development & Multipurpose use system according to claim 1, which is characterized in that the SO2Conversion
Device (17) is vertical vessel, inside sets three layers of catalyst bed, every layer of catalyst bed is respectively arranged below with interlayer cooling device.
7. being handled and being applied for sulfur-containing gas Development & Multipurpose use system using described in as above any claim
Technique, which comprises the steps of:
Step 1: sulfur-containing gas first pass through gravity separator (1) remove the drop wherein carried secretly and solid impurity again into
Enter the absorbing liquid counter current contacting in absorption tower (2) and tower, removes H2S and CO2, net after the desulfurization that absorption tower (2) tower top ejects
Change natural gas isolated after the purge gas separator (3) of outlet take liquid and impurity after into LNG liquefaction system；From absorption tower
(2) richness that tower bottom comes out is molten, first passes through flash tank (4) and flashes away the hydro carbons of dissolution to enter acid gas incinerator (15) oxygen-excess combustion raw
At SO2；
Step 2: the rich solution after flash tank (4) flash distillation enters lean/rich liquid heat exchanger after filter (5) filters out impurity
(6) enter regenerator (7) after being warming up to 105 DEG C, rich solution is contacted with upstream high-temperature steam in regenerator (7) and desorbed
H2S and CO2；120 DEG C of semi lean solutions that regenerator (7) tower bottom comes out enter reboiler (8) and further remove H2S and CO2, remove H2S
And CO2Lean solution by after lean pump (9) pressurization after lean/rich liquid heat exchanger (6) is cooling, then again through lean solution cooler cold (10)
Absorption tower (2) circulation desulfurization is sent by doctor solution circulating pump (11) after cooling；The acid gas desorbed from regenerator (7) enters
The cooling recycling lean solution of acid gas cooler (12), lean solution enters the reflux pump that return tank (13) is arranged by reflux pot bottom after cooling
(14) regenerator (7) are delivered to and carry out recycling and reusing；
Step 3: the concentrate sour gas being discharged at the top of return tank (13) enters acid gas incinerator (15), and sour gas is in acid gas
Oxygen-excess combustion is carried out in incinerator generates SO2, SO in acid gas incinerator (15)2Gas crosses the heat exchange of furnace (16) by waste heat boiler
Enter SO after cooling2Converter (17), in SO2Converter (17) interior SO2It is converted into SO under the action of catalyst3；
Step 4: after temperature is down to sulfuric acid vapor dew point, SO3Gas enters condensation of sulfuric acid device (18), in condensation of sulfuric acid device (18)
SO3Gas and water vapour flow up in tube side occurs hydration reaction generation H2SO4, and as the reduction of temperature is condensed into matter
The liquid heat sulfuric acid of score 98% is measured, hot sulfuric acid temperature is 246 DEG C or so, is passed through again after heat exchanger one (19) drops to 150 DEG C
It crosses heat exchanger two (20) heat exchange and is cooled to 40 DEG C or so rear entrance sulfuric acid storage tank (21), it is then periodically outer by sulfuric acid pump (22) entrucking
It is defeated；
Step 5: the gas being discharged at the top of condensation of sulfuric acid device (18) enters acid mist eliminator (23), in acid mist eliminator (23)
The cold sulfuric acid counter current contacting that gas and sulfuric acid circulating pump (25) are sprayed into from top realizes the condensation recycling of sulfuric acid vapor, fixed gas
Body is discharged into atmosphere from chimney (24)；
Step 6: the fresh air that air blower (26) blasts first passes around heat exchanger two (20) to from heat exchanger one (19)
150 DEG C of sulfuric acid is cooled down again, comes from SO subsequently into condensation of sulfuric acid device (18) top and condensation of sulfuric acid device (18) lower part2
The SO of converter (17)3Heat exchange, which is carried out, with vapor realizes SO3With the hydration reaction of vapor, then from condensation of sulfuric acid device
(18) enter acid gas incinerator after the discharge of bottom and reacted with the concentrate acid gas generation oxygen-excess combustion that return tank (13) top is discharged, it is real
Existing H2S is converted into SO2；
Step 7: enter the solidifying gas steam turbine of afterheat generating system by the middle super pressure-high temperature steam being discharged at the top of waste heat boiler (16)
(27), it is generated electricity by generator (29), hot steam is pressed through in realization by thermal energy and is converted into electric energy；Middle super pressure-high temperature steam is by solidifying
Temperature drops to 100 DEG C hereinafter, realizing the condensation of steam to gas steam turbine (27) afterwards, and steam enters lime set water tank (28) and realizes condensed water
Recycling, the condensed water of recycling by entering heat exchanger one (19) after condensate pump (29) pressurization, then by heat exchanger one (19) into
Enter condensation of sulfuric acid device (18), cools down to the hot sulfuric acid in condensation of sulfuric acid device (18)；Condensation in heat exchanger one (19) simultaneously
Enter the reboiler (8) of amine desulfurization decarbonization system after water heating for the heating to reboiler (8) interior semi lean solution, acceleration half is poor
The sour gas dissolved and absorbed in liquid desorbs, and the condensed water in reboiler (8) is through SO2Converter (17) enters waste heat boiler (16)
It recycles；
Step 8: the purified natural gas come out from purge gas separator (3) enters desulfurization pretreatment device (14), locates in advance in desulfurization
It is dehydrated in reason device (14), desulfurization, demercuration, several grades that pretreated purified natural gas enters LNG liquefaction system are changed
Cool down after hot device, then enters LNG storage tank (45) after the natural gas that whole grade gas-liquid separator (44) cannot not isolated solidifyingly and formed
It is defeated outside finished product LNG, not solidifying natural gas enter after compressor (43) pressurization acid gas incinerator (15) used as fuel gas or into
The first-class heat exchanger entrance for entering LNG liquefaction system is liquefied again.
8. being used for sulfur-containing gas Development & Multipurpose use system and technique according to claim 7, which is characterized in that described
Absorbing liquid in absorption tower (2) is the aqueous solution that concentration is 40~45%MDEA, and absorption tower (2) interior pressure is 3.5~4.0Mpa.
9. being used for sulfur-containing gas Development & Multipurpose use system and technique according to claim 7, which is characterized in that described
SO2Catalyst in reactor (17) is V2O5。
10. being used for sulfur-containing gas Development & Multipurpose use system and technique according to claim 7, which is characterized in that described
Waste heat boiler (16) at the top of be discharged middle super pressure-high temperature steam temperature be 420 DEG C, pressure 3.9Mpa.
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| CN115537298A (en) * | 2022-09-15 | 2022-12-30 | 北京时代桃源环境科技股份有限公司 | Kitchen waste anaerobic methane synchronous desulfurization and decarburization process |
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