CN101054165A - Device and method of reclaim and processing tail gas of sulfur - Google Patents
Device and method of reclaim and processing tail gas of sulfur Download PDFInfo
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- CN101054165A CN101054165A CNA2007100483609A CN200710048360A CN101054165A CN 101054165 A CN101054165 A CN 101054165A CN A2007100483609 A CNA2007100483609 A CN A2007100483609A CN 200710048360 A CN200710048360 A CN 200710048360A CN 101054165 A CN101054165 A CN 101054165A
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- 238000000034 method Methods 0.000 title claims abstract description 91
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 239000011593 sulfur Substances 0.000 title claims abstract description 39
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 39
- 239000007789 gas Substances 0.000 claims abstract description 137
- 230000008569 process Effects 0.000 claims abstract description 83
- 239000001257 hydrogen Substances 0.000 claims abstract description 42
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 42
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000011084 recovery Methods 0.000 claims abstract description 35
- 239000005864 Sulphur Substances 0.000 claims abstract description 33
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 238000010521 absorption reaction Methods 0.000 claims abstract description 31
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 30
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 30
- 238000010791 quenching Methods 0.000 claims abstract description 25
- 239000006096 absorbing agent Substances 0.000 claims abstract description 19
- 239000002918 waste heat Substances 0.000 claims abstract description 19
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 15
- 239000002253 acid Substances 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 41
- 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 18
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims description 18
- 230000009467 reduction Effects 0.000 claims description 18
- 239000003054 catalyst Substances 0.000 claims description 15
- 238000009833 condensation Methods 0.000 claims description 13
- 230000005494 condensation Effects 0.000 claims description 13
- 230000004044 response Effects 0.000 claims description 12
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- 238000010304 firing Methods 0.000 claims description 6
- 239000002737 fuel gas Substances 0.000 claims description 6
- 230000008859 change Effects 0.000 claims description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 239000003546 flue gas Substances 0.000 claims description 3
- 230000008929 regeneration Effects 0.000 claims description 3
- 238000011069 regeneration method Methods 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000004073 vulcanization Methods 0.000 claims description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 8
- 238000006555 catalytic reaction Methods 0.000 abstract 2
- 239000007788 liquid Substances 0.000 abstract 2
- 238000005516 engineering process Methods 0.000 description 8
- 230000008878 coupling Effects 0.000 description 5
- 238000010168 coupling process Methods 0.000 description 5
- 238000005859 coupling reaction Methods 0.000 description 5
- 238000003303 reheating Methods 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical group C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 3
- GVGLGOZIDCSQPN-PVHGPHFFSA-N Heroin Chemical group O([C@H]1[C@H](C=C[C@H]23)OC(C)=O)C4=C5[C@@]12CCN(C)[C@@H]3CC5=CC=C4OC(C)=O GVGLGOZIDCSQPN-PVHGPHFFSA-N 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- -1 sulphur compound Chemical class 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
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- 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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- Treating Waste Gases (AREA)
Abstract
A sulfur recovery and offgas processing device and a method therefor is characterized in that the device comprises a thermal reaction section, a catalytic reaction section and a reducing absorption section. In the thermal reaction section, hydrogen sulfide acid gas is partly burnt in a main burner (1) to convert into sulfur dioxide, hydrogen sulfide and sulfur dioxide proceed claus reaction to generate process gas such as elemental sulphur, the process gas is cooled by a waste-heat boiler (2) and a primary condensate cooler (3) to obtain liquid sulfur; in the catalytic reaction section, the process gas is reacted through a primary reheat hydrogen furnace (4), a secondary steam reheater (7), two stage reactor (5, 8), then separating liquid sulfur is cooled by two stage condensate cooler (6, 9) then enters into the reducing absorption section; in the reducing absorption section, the process gas is heated by a steam heater (10) then hydrogenizated in a hydrogenation reactor (11), cooled in a process gas cooler (12) and enters into a quench tower (13) which top connecting with bottom of a absorber (16), top of the absorber connects with a incinerator (18), the incinerator connects with a chimney (19).
Description
Technical field
The present invention relates to the method for a kind of sulphur recovery and exhaust gas processing device and sulphur recovery thereof and vent gas treatment, belong to sulphur recovery and vent gas treatment field.
Background technology
Along with science and technology development, China is increasing to the demand of oil, Sweet natural gas, and sulfur-bearing in part oil, the Sweet natural gas in order to produce clean energy, needs sulphur is removed, and normally the form with hydrogen sulfide takes off.In handling hydrogen sulfide containing acid gas technology, mainly be as far as possible hydrogen sulfide to be converted into elementary sulfur at present, both economical treatment process is that sulfur recovery rate is about 99%, but can't satisfy the requirement of existing national environmental standard GB16297 " discharge standard of air pollutants ", promptly in the discharging waste gas content of sulfurous gas smaller or equal to 960mg/m
3The main treatment process that can satisfy the national environmental standard requirement is the reduction absorption process, be about to the process gas that conventional sulfur recovery facility comes out and carry out hydrotreatment, make the sulphur compound in the process gas be converted into hydrogen sulfide, by solvent absorption hydrogen sulfide is reclaimed then, returning sulfur recovery facility again handles again, to guarantee that content of sulfur dioxide satisfies national environmental standard in the discharging waste gas, relatively such technology of typical case is SCOT technology, HCR technology.
The ratio of hydrogen sulfide and sulfurous gas is 2 in the process gas that SCOT technology controlling and process sulfur recovery facility comes out, in vent gas treatment online SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE is set partly, producing the part reducing gas uses for process gas hydrogenation, the required hydrogen of hydrogenation is from two aspects, the hydrogen that one side produces from sulfur recovery facility, the hydrogen that produces from online SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE on the other hand.Because be subjected to the restriction of hydrogenator temperature in, the hydrogen manufacturing amount of online SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE is limited, under the situation of normal running, the hydrogen that comes from two aspects reaches hydrogenation substantially and uses.When fluctuation of service, it is incomplete hydrogenation very likely to occur, and cause sulfurous gas to penetrate accident, be that sulfurous gas enters follow-up cooling system and MDEA solution absorption system, cause equipment corrosion and solution rotten, when accident was serious, the MDEA solution of possible solution system needed all to change, and financial loss is big.
The ratio of hydrogen sulfide and sulfurous gas is greater than 4 in the process gas that HCR technology controlling and process sulfur recovery facility comes out, in the vent gas treatment part online SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE is not set, the hydrogen that the required hydrogen of hydrogenation all produces from sulfur recovery facility, through measuring and calculating have only when the ratio of hydrogen sulfide and sulfurous gas in the process gas that sulfur recovery facility comes out greater than 10 the time, carry hydrogen sulfide in the process gas that sulfur recovery facility comes out and just reach hydrogenation usefulness, at this moment, the sulfur recovery rate of sulfur recovery facility reduces by 1.5% approximately, and the scale of sulphur recovery and exhaust gas processing device also can increase.When fluctuation of service, it is incomplete hydrogenation very likely to occur, and cause sulfurous gas to penetrate accident, be that sulfurous gas enters follow-up cooling system and MDEA solution absorption system, cause equipment corrosion and solution rotten, when accident was serious, the MDEA solution of possible solution system needed all to change, and financial loss is big.
How to guarantee as far as possible economically that sulphur recovery and exhaust gas processing device sulfurous gas do not take place penetrate accident, be a great problem that faces in the execute-in-place process always.People urgently wish head it off.
Summary of the invention
The objective of the invention is to provide the method for a kind of sulphur recovery and exhaust gas processing device and sulphur recovery and vent gas treatment at the deficiencies in the prior art.Be characterized in the hydrogen sulfide in the sulfide hydrogen acid gas is converted into Molten sulphur, the sulfurous gas sulphur concentration in the exhaust emissions is up to state standards.
Purpose of the present invention is realized by following technical measures
Sulphur recovery and exhaust gas processing device contain thermal response section, catalyst reaction section and reduction absorber portion, the thermal response section contains main burning furnace, waste heat boiler and one-level condensate cooler, main burning furnace one end is connected with blast main with hydrogen sulfide acid gas pipe, the other end is connected with the one-level condensate cooler by waste heat boiler, one-level condensate cooler lower end and molten sulfur pipe coupling, one-level condensate cooler upper end is connected with the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level; Catalyst reaction section contains double reheating device, two-stage reactor and condensed in two stages water cooler, process gas enters the reduction absorber portion through double reheating device and reactor reaction after the refrigerated separation Molten sulphur, the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level is connected with A reactor, A reactor is connected with the B-grade condensation water cooler, B-grade condensation water cooler lower end and molten sulfur pipe coupling, the second steam well heater is connected with second reactor, second reactor is connected with three grades of condensate coolers, three grades of condensate cooler lower ends and molten sulfur pipe coupling; The reduction absorber portion contains steam heater, hydrogenator, process gas water cooler, quench tower, the absorption tower, incinerator and chimney, three grades of condensate cooler upper ends are connected with hydrogenator by steam heater, hydrogenator is connected with quench tower through water cooler, the quench tower bottom is connected with the inlet of sour water recycle pump, the sour water pump discharge respectively with sour water water cooler and sour water pipe coupling, the quench tower top is connected with the bottom, absorption tower, be connected with the rich MDEA solution conduit of desulfurizer by the rich solution pump in the bottom, absorption tower, the poor MDEA solution conduit of desulfurizer is connected with top, absorption tower, the top, absorption tower is connected with incinerator, and incinerator is connected with chimney.
The hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of main burning furnace, one-level is connected with blast main with fuel gas pipe respectively with incinerator.The hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level also with the low-pressure steam pipe coupling.
In A reactor, second reactor and the hydrogenator catalyzer is housed, its temperature in is controlled to be 200 ℃～350 ℃, 180 ℃～250 ℃, 180 ℃～250 ℃ respectively.
Hydrogenator is connected with steam heater.
The temperature out of hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of main burning furnace, one-level and incinerator can be controlled to be 900 ℃～1300 ℃, 200 ℃～350 ℃, 400 ℃～800 ℃ respectively.
The sulphur recovery of a kind of sulphur recovery and exhaust gas processing device and the method for vent gas treatment:
1, thermal response section:
(1) mixed firing in main burning furnace with acid gas and air, the control temperature of combustion is at 900 ℃～1300 ℃, make partial vulcanization hydrogen change into sulfurous gas, and claus reaction at high temperature takes place, most of hydrogen sulfide and sulfurous gas reaction generting element sulphur form the process gas that contains hydrogen sulfide, elementary sulfur, sulfurous gas component;
(2) process gas enters waste heat boiler, waste heat boiler produces the middle pressure steam of 3.5MPa～4.5MPa, the process gas of process waste heat boiler enters the one-level condensate cooler and is cooled to 150 ℃～180 ℃ of temperature, isolates molten sulfur, and the one-level condensate cooler produces the low-pressure steam of 0.5MPa;
(3) middle pressure steam of waste heat boiler generation 3.5MPa～4.5MPa uses for catalyst reaction section, reduction absorber portion, and the process gas that comes out from the one-level condensate cooler enters catalyst reaction section;
2, catalyst reaction section:
(1) the process gas that comes out from the thermal response section enters the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level, in process gas, allocate air into, the hydrogen that the part of fuel gas firing is produced is used for reduction absorber portion hydrogenation, process gas enters A reactor after being heated to 200 ℃～350 ℃ with middle pressure steam, by regulating the air add-on hydrogen sulfide in the process gas of three grades of condensate cooler outlets and the ratio of sulfurous gas is controlled at 4～8.
(2) process gas is proceeded claus reaction in A reactor, enters the B-grade condensation water cooler then and is cooled to 150 ℃～180 ℃ of temperature, isolates molten sulfur, and produces the low-pressure steam of 0.5MPa;
(3) the process gas by the B-grade condensation water cooler enters the second steam well heater, enters second reactor after being heated to 180 ℃～250 ℃ of temperature with middle pressure steam;
(4) the process gas in second reactor is proceeded claus reaction, enters to isolate molten sulfur after three grades of condensate coolers are cooled to 150 ℃～180 ℃ of temperature, produces the low-pressure steam of 0.5MPa;
3, reduction absorber portion:
(1) the process gas that comes out from three grades of condensate coolers enters steam heater, is heated to enter after 180 ℃～250 ℃ of the temperature with middle pressure steam and carries out hydrogenation reaction in the hydrogenator;
(2) the process gas that comes out from hydrogenator enters process gas water cooler and is cooled to and enters quench tower after 150 ℃～200 ℃ of the temperature and further cool off, sour water a part of carrying device behind the sour water recycle pump of quench tower bottom, a part is sent into the quench tower top and is recycled after the cooling of sour water water cooler, the process gas that quench tower comes out enters the absorption tower, by poor MDEA solution counter current contact, hydrogen sulfide in the subtractive process gas, hydrogen sulfide content is below 250ppm in the control process gas;
(3) the process gas that comes out from the absorption tower enters incinerator and burns, incineration temperature is 400 ℃～800 ℃, all sulphur and sulfide all are converted into sulfurous gas, the flue gas that comes out from incinerator enters atmosphere by chimney, and the rich MDEA solution that comes out from the absorption tower is pumped to desulfurizer regeneration through rich solution.
The present invention has following advantage:
Sulfur dioxide concentration in 1 exhaust emissions reaches the GB16297 national standard.
The 2 pairs of Gas Purification Factory and smoke processing system have extensive applicability.
3 have reduced the required amounts of hydrogen of tail gas hydrogenation, thereby have reduced the risk that sulfurous gas penetrates, safe and reliable.
The self-produced steam of 4 these devices has been saved the energy as the heating thermal source, has reduced cost.
5 have cancelled online SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE, adopt steam as process gas thermal source again, have simplified flow process, have reduced the process airshed, have dwindled the size of equipment; Saved investment, easy to operate.
Description of drawings
Fig. 1 is the structural representation of sulphur recovery and exhaust gas processing device
1 main burning furnace, 2 waste heat boilers, 3 one-level condensate coolers, the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of 4 one-levels, 5 A reactors, 6 B-grade condensation water coolers, 7 second steam reheaters, 8 second reactors, 9 three grades of condensate coolers, 10 steam heaters, 11 hydrogenators, 12 process gas water coolers, 13 quench towers, 14 sour water recycle pumps, 15 sour water water coolers, 16 absorption towers, 17 rich solution pumps, 18 incinerators, 19 chimneys, 20 gas line, 21 blast mains, 22 molten sulfur pipes, 23 low pressure steam pipes, the rich MDEA solution conduit of 24 desulfurizers, the poor MDEA solution conduit of 25 desulfurizers, 26 sour water pipes, 27 acid gas pipes.
Embodiment
Below by embodiment the present invention is specifically described; be necessary to be pointed out that at this following examples only are used for the present invention is further specified; can not be interpreted as limiting the scope of the invention, the person skilled in the art in this field can make some nonessential improvement and adjustment according to the content of the invention described above.
The sulphur recovery of reheating furnace hydrogen manufacturing and exhaust gas processing device have simple in structure, easily manufactured, as shown in Figure 1, this device contains thermal response section, catalyst reaction section and reduction absorber portion, the thermal response section contains main burning furnace 1, waste heat boiler 2 and one-level condensate cooler 3, main burning furnace 1 one ends are connected with blast main 21 with hydrogen sulfide acid gas pipe 27, the other end is connected with one-level condensate cooler 3 by waste heat boiler 2, one-level condensate cooler lower end is connected with molten sulfur pipe 22, and one-level condensate cooler upper end is connected with the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE 4 of one-level; Catalyst reaction section contains double reheating device, two-stage reactor and condensed in two stages water cooler, process gas enters the reduction absorber portion through double reheating device and reactor reaction after the refrigerated separation Molten sulphur, the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE 4 of one-level is connected with A reactor 5, A reactor is connected with B-grade condensation water cooler 6, B-grade condensation water cooler lower end is connected with molten sulfur pipe 22, second steam well heater 7 is connected with second reactor 8, second reactor is connected with three grades of condensate coolers 9, and three grades of condensate cooler lower ends are connected with molten sulfur pipe 22; The reduction absorber portion contains steam heater 10, hydrogenator 11, process gas water cooler 12, quench tower 13, absorption tower 16, incinerator 18 and chimney 19, three grades of condensate cooler 9 upper ends are connected with hydrogenator 11 by steam heater 10, hydrogenator is connected with quench tower 13 through water cooler 12, the quench tower bottom is connected with the inlet of sour water recycle pump 14, the sour water pump discharge is connected with sour water pipe 26 with sour water water cooler 15 respectively, the quench tower top is connected with 16 bottoms, absorption tower, be connected with the rich MDEA solution conduit 25 of desulfurizer by rich solution pump 17 in the bottom, absorption tower, the poor MDEA solution conduit 24 of desulfurizer is connected with top, absorption tower, the top, absorption tower is connected with incinerator 18, and incinerator is connected with chimney 19.
The hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE 4 of main burning furnace 1, one-level is connected with blast main 21 with fuel gas pipe 20 respectively with incinerator 18.The hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE 4 of one-level also is connected with low pressure steam pipe 23.
In A reactor, second reactor and the hydrogenator catalyzer is housed, its temperature in is controlled to be 200 ℃～350 ℃, 180 ℃～250 ℃, 180 ℃～250 ℃ respectively.
The temperature out of hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE 4 of main burning furnace 1, one-level and incinerator 18 can be controlled to be 900 ℃～1300 ℃, 200 ℃～350 ℃, 400 ℃～800 ℃ respectively.
Hydrogenator is connected with steam heater.
The temperature out of hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of main burning furnace, one-level and incinerator can be controlled to be 900 ℃～1300 ℃, 200 ℃～350 ℃, 400 ℃～800 ℃ respectively.
The sulphur recovery of sulphur recovery and exhaust gas processing device and the method for vent gas treatment:
1, thermal response section:
(1) mixed firing in main burning furnace 1 with acid gas and air, the control temperature of combustion is at 900 ℃～1300 ℃, make partial vulcanization hydrogen change into sulfurous gas, and claus reaction at high temperature takes place, most of hydrogen sulfide and sulfurous gas reaction generting element sulphur form the process gas that contains hydrogen sulfide, elementary sulfur, sulfurous gas component;
(2) process gas enters waste heat boiler 2, waste heat boiler produces the middle pressure steam of 3.5MPa～4.5MPa, the process gas of process waste heat boiler enters one-level condensate cooler 3 and is cooled to 150 ℃～180 ℃ of temperature, isolates molten sulfur, and the one-level condensate cooler produces the low-pressure steam of 0.5MPa;
(3) middle pressure steam of waste heat boiler generation 3.5MPa～4.5MPa uses for catalyst reaction section, reduction absorber portion, and the process gas that comes out from the one-level condensate cooler enters catalyst reaction section;
2, catalyst reaction section:
(1) the process gas that comes out from the thermal response section enters the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE 4 of one-level, in process gas, allocate air into, the hydrogen that the part of fuel gas firing is produced is used for reduction absorber portion hydrogenation, process gas enters A reactor 5 after being heated to 200 ℃～350 ℃ with middle pressure steam, by regulating the air add-on hydrogen sulfide in the process gas of three grades of condensate coolers, 9 outlets and the ratio of sulfurous gas is controlled at 4～8.
(2) process gas is proceeded claus reaction in A reactor, enters B-grade condensation water cooler 6 then and is cooled to 150 ℃～180 ℃ of temperature, isolates molten sulfur, and produces the low-pressure steam of 0.5MPa;
(3) the process gas by the B-grade condensation water cooler enters second steam well heater 7, enters second reactor 8 after being heated to 180 ℃～250 ℃ of temperature with middle pressure steam;
(4) the process gas in second reactor is proceeded claus reaction, enters to isolate molten sulfur after three grades of condensate coolers 9 are cooled to 150 ℃～180 ℃ of temperature, produces the low-pressure steam of 0.5MPa;
3, reduction absorber portion:
(1) the process gas that comes out from three grades of condensate coolers enters steam heater 10, is heated to enter after 180 ℃～250 ℃ of the temperature with middle pressure steam and carries out hydrogenation reaction in the hydrogenator 11;
(2) the process gas that comes out from hydrogenator enters process gas water cooler 12 and is cooled to and enters quench tower 13 after 150 ℃～200 ℃ of the temperature and further cool off, sour water a part of carrying device behind sour water recycle pump 14 of quench tower bottom, a part is sent into the quench tower top and is recycled after 15 coolings of sour water water cooler, the process gas that quench tower comes out enters absorption tower 16, by poor MDEA solution counter current contact, hydrogen sulfide in the subtractive process gas, hydrogen sulfide content is below 250ppm in the control process gas;
(3) the process gas that comes out from the absorption tower enters incinerator 18 and burns, incineration temperature is 400 ℃～800 ℃, all sulphur and sulfide all are converted into sulfurous gas, the flue gas that comes out from incinerator enters atmosphere by chimney 19, and the rich MDEA solution that comes out from the absorption tower is delivered to desulfurizer regeneration through rich solution pump 17.
Claims (6)
1, a kind of sulphur recovery and exhaust gas processing device, it is characterized in that this device contains thermal response section, catalyst reaction section and reduction absorber portion, the thermal response section is to be connected with blast main (21) with hydrogen sulfide acid gas pipe (27) by main burning furnace (1) one end, the other end is connected with one-level condensate cooler (3) by waste heat boiler (2), one-level condensate cooler lower end is connected with molten sulfur pipe (22), and the one-level condensate cooler is connected with the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level (4); Catalyst reaction section is to be connected with A reactor (5) by the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level (4), A reactor is connected with B-grade condensation water cooler (6), B-grade condensation water cooler lower end is connected with molten sulfur pipe (22), second steam well heater (7) is connected with second reactor (8), second reactor is connected with three grades of condensate coolers (9), and three grades of condensate cooler lower ends are connected with molten sulfur pipe (22); The reduction absorber portion is to be connected with hydrogenator (11) by steam heater (10) by three grades of condensate coolers (9) upper end, hydrogenator is connected with quench tower (13) through water cooler (12), the quench tower bottom is connected with the inlet of sour water recycle pump (14), the sour water pump discharge is connected with sour water pipe (26) with sour water water cooler (15) respectively, the quench tower top is connected with bottom, absorption tower (16), be connected with the rich MDEA solution conduit (25) of desulfurizer by rich solution pump (17) in the bottom, absorption tower, the poor MDEA solution conduit (24) of desulfurizer is connected with top, absorption tower, the top, absorption tower is connected with incinerator (18), and incinerator is connected with chimney (19).
2, sulphur recovery and exhaust gas processing device according to claim 1, it is characterized in that main burning furnace (1), the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level (4) and incinerator (18) are connected with blast main (21) with fuel gas pipe (20) respectively, the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level (4) also is connected with low pressure steam pipe (23).
3, sulphur recovery and exhaust gas processing device according to claim 1, it is characterized in that in A reactor, second reactor and the hydrogenator catalyzer being housed, its temperature in is controlled to be 200 ℃～350 ℃, 180 ℃～250 ℃, 180 ℃～250 ℃ respectively.
4, sulphur recovery and exhaust gas processing device according to claim 1 is characterized in that hydrogenator (11) is connected with steam heater (10).
5, sulphur recovery and exhaust gas processing device according to claim 1, it is characterized in that main burning furnace (1), the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level (4), and the temperature out of incinerator (18) can be controlled to be 900 ℃～1300 ℃, 200 ℃～350 ℃, 400 ℃～800 ℃ respectively.
6, the method for the sulphur recovery of a kind of sulphur recovery and exhaust gas processing device and vent gas treatment is characterized in that:
1), thermal response section:
(1) mixed firing in main burning furnace (1) with acid gas and air, the control temperature of combustion is at 900 ℃～1300 ℃, make partial vulcanization hydrogen change into sulfurous gas, and claus reaction at high temperature takes place, most of hydrogen sulfide and sulfurous gas reaction generting element sulphur form the process gas that contains hydrogen sulfide, elementary sulfur, sulfurous gas component;
(2) process gas enters waste heat boiler (2), waste heat boiler produces the middle pressure steam of 3.5MPa～4.5MPa, the process gas of process waste heat boiler enters one-level condensate cooler (3) and is cooled to 150 ℃～180 ℃ of temperature, isolates molten sulfur, and the one-level condensate cooler produces the low-pressure steam of 0.5MPa;
(3) middle pressure steam of waste heat boiler generation 3.5MPa～4.5MPa uses for catalyst reaction section, reduction absorber portion, and the process gas that comes out from the one-level condensate cooler enters catalyst reaction section;
2), catalyst reaction section:
(1) the process gas that comes out from the thermal response section enters the hot again SECTION TUBE FOR HYDROGEN MANNU-FACTURING FURNACE of one-level (4), in process gas, allocate air into, the hydrogen that the part of fuel gas firing is produced is used for reduction absorber portion hydrogenation, process gas enters A reactor (5) after being heated to 200 ℃～350 ℃ with middle pressure steam, by regulating the air add-on hydrogen sulfide in the process gas of three grades of condensate coolers (9) outlet and the ratio of sulfurous gas is controlled at 4～8.
(2) process gas is proceeded claus reaction in A reactor, enters B-grade condensation water cooler (6) then and is cooled to 150 ℃～180 ℃ of temperature, isolates molten sulfur, and produces the low-pressure steam of 0.5MPa;
(3) the process gas by the B-grade condensation water cooler enters second steam well heater (7), enters second reactor (8) after being heated to 180 ℃～250 ℃ of temperature with middle pressure steam;
(4) the process gas in second reactor is proceeded claus reaction, enters to isolate molten sulfur after three grades of condensate coolers (9) are cooled to 150 ℃～180 ℃ of temperature, produces the low-pressure steam of 0.5MPa;
3), reduction absorber portion:
(1) the process gas that comes out from three grades of condensate coolers enters steam heater (10), is heated to enter in the hydrogenator (11) after 180 ℃～250 ℃ of the temperature with middle pressure steam and carries out hydrogenation reaction;
(2) the process gas that comes out from hydrogenator enters and enters further cooling of quench tower (13) after process gas water cooler (12) is cooled to 150 ℃～200 ℃ of temperature, sour water a part of carrying device behind sour water recycle pump (14) of quench tower bottom, a part is sent into the quench tower top and is recycled after sour water water cooler (15) cooling, the process gas that quench tower comes out enters absorption tower (16), by poor MDEA solution counter current contact, hydrogen sulfide in the subtractive process gas, hydrogen sulfide content is below 250ppm in the control process gas;
(3) the process gas that comes out from the absorption tower enters incinerator (18) and burns, incineration temperature is 400 ℃～800 ℃, all sulphur and sulfide all are converted into sulfurous gas, the flue gas that comes out from incinerator enters atmosphere by chimney (19), and the rich MDEA solution that comes out from the absorption tower is delivered to desulfurizer regeneration through rich solution pump (17).
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