CN102530882B - Method and device for reclaiming dehydrated sulfur - Google Patents
Method and device for reclaiming dehydrated sulfur Download PDFInfo
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- CN102530882B CN102530882B CN2010106164312A CN201010616431A CN102530882B CN 102530882 B CN102530882 B CN 102530882B CN 2010106164312 A CN2010106164312 A CN 2010106164312A CN 201010616431 A CN201010616431 A CN 201010616431A CN 102530882 B CN102530882 B CN 102530882B
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Abstract
The invention relates to a method and a device for reclaiming dehydrated sulfur. The method comprises the following steps of: reacting acid gas and air in a combustion furnace, and cooling the process gas to the temperature of 315 DEG C through a waste heat boiler; feeding the process gas into a gas/ gas heat exchanger, and performing heat exchange with process gas at a quenching tower outlet to cool the fed process gas to the temperature of 272.3 DEG C; cooling the process gas to the temperature of 164 DEG C in a primary condenser, and condensing and separating sulfur steam; cooling the process gas to the temperature of between 35 and 60 DEG C in a quenching tower circulating device, and performing heat exchange on the cooled process gas and the process gas from the gas/ gas heat exchanger and the waste heat boiler outlet so that the temperature of the cooled process gas is raised to 100 DEG C; and feeding the process gas into a catalytic conversion system through a primary online combustion furnace, reacting SO2 and H2S to generate elemental sulfur, and condensing and separating sulfur steam. By the method, the consumption of a fuel for the primary online combustion furnace is reduced, the treatment quantity of the process gas is reduced, the conversion rate of sulfur in a downstream Klaus device is improved due to reduction of the water vapor and the sulfur steam in the process gas, and the reclaiming rate of the total process sulfur is further improved.
Description
Technical field
The present invention relates to a kind of type sulfur recovery method and device of dewatering, be applicable to process high sulphur-containing gas.Belong to the natural gas processing field.
Background technology
In recent years, the environmental protection based on increasingly stringent needs recovery sulphur from Sweet natural gas and refinery gas, minimizing SO
2Sulfur recovery and the tail gas treatment process of quantity discharged have obtained tremendous development.In simple terms, sub-dewpoint process take CBA, MCRC, Clinsulf-SDP, Sulfreen and Clauspol etc. as representative is arranged, direct oxidation process take Clinsulf-DO, ENsulf, Selectox, Superclaus and Modop etc. as representative, the oxygen enriching process take Oxyclaus, Sure and COPE etc. as representative and the Reducing and absorption technique take SCOT, BSRP, LTGT, Resulf and RAR etc. as representative.Also have in addition the oxidation absorption technique take Wellman-Lord technique and Cansolv technique as representative, because technical process is comparatively complicated, equipment corrosion is comparatively serious, uses few.
From present applicable cases, use maximum be Reducing and absorption technique, secondly be sub-dewpoint process, be direct oxidation process again, be oxygen enriching process at last.The oxidation absorption technique almost has no formal industrial application report.In general, usually contain a large amount of water vapour and be on a small quantity sulfur vapor under the state of saturation in the Cross unit Process Gas.The two is as the resultant of claus reaction, and the higher claus reaction sulphur of its concentration transformation efficiency is less.In whole Cross unit, do not remove water vapour, thereby the continuous accumulation of the water vapour that generates along with claus reaction, reactor inlet Process Gas water vapour contents at different levels constantly increase.Go out in typical case the Process Gas water vapour content of last step reactor usually up to 20～30%.Be subjected to the restriction of Crouse's balanced reaction, the total sulphur rate of recovery of technique has been subject to impact to a certain degree.
Summary of the invention
The purpose of this invention is to provide a kind of type sulfur recovery facility that dewaters.Adopted the sulphur removal recycle system that dewaters---the quench tower device, can effectively reduce the water vapour and the sulfur vapor that contain in the Process Gas.Be provided with the Process Gas primary heater unit in the quench tower outlet, the preheating thermal source has reduced the usage quantity of the online roasting kiln fuel gas of one-level from waste heat boiler exit procedure gas.
A kind of type sulfur recovery facility that dewaters of the present invention comprises high-temp combustion part, condensation portion, except water section, again heat, regenerator section and catalytic conversion part.Acid gas and air mixed in main burning furnace are carried out the high temperature claus reaction; One cover gas/gas interchanger is set behind waste heat boiler, and waste heat boiler exit procedure gas is as quench tower exit procedure gas preheating thermal source.Gas/gas heat exchanger exit Process Gas is through the first-stage condenser cooling and isolate molten sulfur; First-stage condenser exit procedure gas enters quench tower and is cooled to lesser temps, a large amount of water vapor condensations are liquid water in the Process Gas, be on a small quantity sulfur vapor under the state of saturation and then sublimate and be solid-state sulphur, and then reduced the content of water vapour in the Process Gas, and isolate the sulphur that generates in the roasting kiln fully.Crouse's balanced reaction is carried out towards the direction that is conducive to generate sulphur in the downstream unit.Quench tower exit procedure gas enters gas/gas interchanger, and comes to carry out heat exchange to waste heat boiler outlet pyroprocess gas.Reduce the cooling load of first-stage condenser and quench tower, reduced the fuel usage quantity of the online roasting kiln of one-level.H in the Process Gas
2S, SO
2Claus reaction further occurs in downstream unit, and the content of water vapour and sulfur vapor is reduced in the one-level convertor entry process gas, and downstream unit sulphur transformation efficiency is improved.
Method steps is described below: the acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln, and out pyroprocess gas is cooled to 315 ℃ through waste heat boiler in main burning furnace; Enter gas/gas interchanger from waste heat boiler Process Gas out, carry out heat exchange temperature with quench tower exit procedure gas and be down to 272.3 ℃; Process Gas after heat exchange enters first-stage condenser and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; Enter the quench tower circulation device from first-stage condenser Process Gas out, Process Gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is on a small quantity state of saturation is all sublimated and is solid-state sulphur; Carry out heat exchange from quench tower Process Gas out through gas/gas interchanger and waste heat boiler exit procedure gas, temperature is increased to 100 ℃; Process Gas after the preheating enters the online roasting kiln of one-level; Enter one-level catalytic converter, SO from the online roasting kiln of one-level Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter the secondary condenser cooling from one-level catalytic converter Process Gas out, sulfur vapor obtains condensation and separates; Enter the online roasting kiln of secondary from secondary condenser Process Gas out; Enter secondary catalytic converter, SO from the online roasting kiln of secondary Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter three grades of condenser coolings from secondary catalytic converter Process Gas out, sulfur vapor obtains condensation and separates; Enter three grades of online roasting kilns from three grades of condensers Process Gas out; Enter the online roasting kiln of level Four from three grades of catalytic converters Process Gas out and an amount of air proportioning; Enter the direct oxidation reactor, the H in the Process Gas from the online roasting kiln of level Four Process Gas out
2The direct oxidation under the effect of catalyzer of S gas is elemental sulfur; Enter last condenser stage from direct oxidation reactor gas out, sulfur vapor obtains condensation and separates.The direct oxidation catalyzer is that ferric oxide is active ingredient take silicon-dioxide as carrier; The used catalyzer of catalytic converter is conventional activated alumina catalyst.
The present invention has following advantage:
1, the present invention is provided with first a cover quench tower device after first-stage condenser, and the Process Gas temperature is down to 35～60 ℃, and making its a large amount of water vapor condensations that contain is liquid water, and the sulfur vapor that is on a small quantity state of saturation is sublimated and is solid-state sulphur.Reduce so that downstream Cross unit sulfur conversion rate improves because of the water vapour that contains and sulfur vapor in the Process Gas, and then increased the total sulphur rate of recovery of technique.
2, the present invention is provided with a cover gas/gas heat-exchanger rig behind quench tower, and quench tower exit procedure gas is carried out preheating, and the preheating thermal source is from waste heat boiler outlet pyroprocess gas.Avoid because of the temperature difference influence operational process of craft, reduce the online roasting kiln fuel of one-level usage quantity, reduced the treatment capacity of technological process gas.
Description of drawings
Fig. 1 is the structural representation that the embodiment of the invention 1 is described.
Shown in Figure 1: 1 main burning furnace, 2 waste heat boilers, 3 gas/gas interchanger, 4 first-stage condenser, 5 for water circle device, 6 secondary condensers, 7 three grades of condensers, 8 level Four condensers, 9 sulphur mist traps, 10 quench towers, the online roasting kiln of 11 one-levels, 12 one-level convertors, 14 secondary convertors, 15 3 grades of online roasting kilns, 16 3 grades of convertors, the online roasting kiln of 17 level Four, 18 super Crouse's convertors, 19 reclamation tail gas burning stoves, 20 chimneys.
Fig. 2 is process program 2 structural representations of the present invention.
Shown in Figure 2: 1 main burning furnace, 2 waste heat boilers, 3 gas/gas interchanger, 4 first-stage condenser, 5 for water circle device, 6 secondary condensers, 7 three grades of condensers, 8 level Four condensers, 9 sulphur mist traps, 10 quench towers, the online roasting kiln of 11 one-levels, 12 one-level convertors, 14 secondary convertors, 16 3 grades of convertors, 19 reclamation tail gas burning stoves, 20 chimneys, 21 gas/gas interchanger, 22 T-valve, 23 T-valve, 24 T-valve.
Fig. 3 is process program 3 structural representations of the present invention.
Shown in Figure 3: 1 main burning furnace, 2 waste heat boilers, 3 gas/gas interchanger, 4 first-stage condenser, 5 for water circle device, 6 secondary condensers, 7 three grades of condensers, 8 level Four condensers, 9 sulphur mist traps, 10 quench towers, the online roasting kiln of 11 one-levels, 12 one-level convertors, the online roasting kiln of 13 secondarys, 14 secondary convertors, 15 3 grades of online roasting kilns, 16 3 grades of convertors, the online roasting kiln of 17 level Four, 19 reclamation tail gas burning stoves, 20 chimneys, 25 quench towers, 26 absorption towers, 27 regenerator columns, 28 hydrogenators.
Fig. 4 is process program 4 structural representations of the present invention.
Shown in Figure 4: 1 main burning furnace, 2 waste heat boilers, 3 gas/gas interchanger, 4 first-stage condenser, 5 for water circle device, 6 secondary condensers, 7 three grades of condensers, 8 level Four condensers, 9 sulphur mist traps, 10 quench towers, the online roasting kiln of 11 one-levels, 12 one-level convertors, the online roasting kiln of 13 secondarys, 14 secondary convertors, 15 3 grades of online roasting kilns, 16 3 grades of convertors, 19 reclamation tail gas burning stoves, 20 chimneys.
Fig. 5 is process program 5 structural representations of the present invention.
Shown in Figure 5: 1 main burning furnace, 2 waste heat boilers, 3 gas/gas interchanger, 4 first-stage condenser, 5 for water circle device, 6 secondary condensers, 7 three grades of condensers, 9 sulphur mist traps, 10 quench towers, the online roasting kiln of 11 one-levels, 12 one-level convertors, the online roasting kiln of 13 secondarys, 14 secondary convertors, 19 reclamation tail gas burning stoves, 20 chimneys.
Fig. 6 is that quench tower dewaters, sulphur removal recycle system schematic diagram.
Shown in Figure 6: 1 main burning furnace, 2 waste heat boilers, 3 gas/gas interchanger, 4 first-stage condenser, 5 for water circle device, 10 quench towers, the online roasting kiln of 11 one-levels, 29 temperature are crossed and the water-content supervisory system, 30 magnetic valves.
Embodiment
The type sulfur recovery facility that dewaters of the present invention is by main burning furnace 1, waste heat boiler 2, gas/gas interchanger 3, condenser, for water circle device 5, sulphur mist trap 9, quench tower 10, online roasting kiln, convertor, super Crouse's convertor 18, reclamation tail gas burning stove 19, chimney 20 consists of; Main burning furnace 1 and waste heat boiler 2 join end to end, and waste heat boiler 2 outlets are connected with gas/gas interchanger 3 tube side entrances, and gas/gas interchanger 3 tube sides outlet is connected with first-stage condenser 4 entrances; First-stage condenser 4 outlets are connected with quench tower 10 bottom inlets; Be connected with the outlet at bottom of quench tower 10 for the entrance of water circle device 5, the outlet of confession water circle device 5 is connected with the upper side entrance of quench tower 10, and connection line is provided with to cross with temperature is connected the magnetic valve 30 that is connected with the water-content supervisory system; The top exit of quench tower 10 is connected with the shell side entrance of gas/gas interchanger 3, and connection line is provided with temperature and crosses and the water-content supervisory system; The shell side outlet of gas/gas interchanger 3 is connected with the online roasting kiln 11 of one-level.See Fig. 6.The online roasting kiln 11 of one-level successively with the reaction of high order system, sulphur mist trap 9, the reclamation tail gas burning stove 19 that are consisted of by convertor, condenser, online roasting kiln, chimney 20 connects.
The below is in conjunction with Fig. 1, and the embodiment of this patent is described.As shown in Figure 1, the acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, are cooled to 315 ℃ from main burning furnace 1 pyroprocess gas out through waste heat boiler 2; Enter gas/gas interchanger 3 from waste heat boiler 2 Process Gas out, carry out heat exchange temperature with quench tower 10 exit procedure gas and be down to 272.3 ℃; Process Gas after heat exchange enters first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; Enter quench tower circulation device 5,10 from first-stage condenser 4 Process Gas out, Process Gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is on a small quantity state of saturation is then all sublimated and is solid-state sulphur; Carry out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas from quench tower 10 Process Gas out, temperature is increased to 100 ℃; Process Gas enters the online roasting kiln 11 of one-level after the preheating, and temperature rises to 220 ℃; Enter one-level catalytic converter 12, SO from the online roasting kiln 11 of one-level Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter secondary condenser 6 from one-level catalytic converter 12 Process Gas out and be cooled to 173 ℃, sulfur vapor obtains condensation and separates; Enter the online roasting kiln 13 of secondary from secondary condenser 6 Process Gas out, temperature rises to 204 ℃; Enter secondary catalytic converter 14, SO from the online roasting kiln 13 of secondary Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter three grades of condensers 7 from secondary catalytic converter 14 Process Gas out and be cooled to 162 ℃, sulfur vapor obtains condensation and separates; Enter three grades of online roasting kilns 15 from three grades of condensers 7 Process Gas out, temperature rises to 220 ℃; Enter the online roasting kiln 17 of level Four from three grades of catalytic converters 16 Process Gas out and an amount of air proportioning, temperature rises to 210 ℃; Enter super Crouse's convertor 18, the H in the Process Gas from the online roasting kiln 17 of level Four Process Gas out
2The direct oxidation under the effect of catalyzer of S gas is elemental sulfur; Enter last condenser stage 8 from super Crouse's convertor 18 gas out, wherein the molten sulfur of condensation is separated; After over cure mist trap 9 captured the sulphur mist that contains in the Process Gas, Process Gas passes into 19 calcinations of reclamation tail gas burning stove, and was emptying by chimney 20.
The below is in conjunction with Fig. 2, and the embodiment of this patent is described.As shown in Figure 2, the acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, are cooled to 315 ℃ from main burning furnace 1 pyroprocess gas out through waste heat boiler 2; Enter gas/gas interchanger 3 from waste heat boiler 2 Process Gas out, carry out heat exchange temperature with quench tower 10 exit procedure gas and be down to 272.3 ℃; Process Gas after heat exchange enters first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; Enter quench tower circulation device 5,10 from first-stage condenser 4 Process Gas out, Process Gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is on a small quantity state of saturation is then all sublimated and is solid-state sulphur; Carry out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas from quench tower 10 Process Gas out, temperature is increased to 100 ℃; Process Gas enters the online roasting kiln 11 of one-level after the preheating, and temperature rises to 279 ℃; Enter one-level catalytic converter 12, SO from the online roasting kiln 11 of one-level Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter gas/gas interchanger 21 tube sides from one-level catalytic converter 12 Process Gas out, tube side exit procedure gas enters secondary condenser 6 and is cooled to 173 ℃, and sulfur vapor obtains condensation and separates; Enter gas/gas interchanger 21 shell sides from secondary condenser 6 Process Gas out, shell side exit procedure gas enters second reactor 14 through T-valve 22, and catalyzer is regenerated, simultaneously SO
2And H
2S generates elemental sulfur in the beds reaction; Enter three grades of condensers 7 from second reactor Process Gas out and be cooled to 126 ℃, sulfur vapor obtains condensation and separates; Enter three reactor 16 through T-valve 23, SO in the Process Gas from three grades of condensers 7 Process Gas out
2And H
2S low-temp reaction on beds generates elemental sulfur; Enter level Four condenser 8 from three reactor 16 Process Gas out and be cooled to 125 ℃, sulfur vapor obtains condensation and separates; Enter sulphur mist trap 9 from level Four condenser 8 Process Gas out through T-valve 24, after over cure mist trap 9 captured the sulphur mist that contains in the Process Gas, Process Gas passes into 19 calcinations of reclamation tail gas burning stove, and was emptying by chimney 20.
Switch: after the switching, gas/gas interchanger 21 shell side mouth Process Gas enter three reactor 16 through T-valve 22 certainly, and catalyzer is regenerated, simultaneously SO
2And H
2S generates elemental sulfur in the beds reaction; Enter level Four condenser 8 from three reactor 16 Process Gas out and be cooled to 126 ℃, sulfur vapor obtains condensation and separates; Enter second reactor 14 from level Four condenser 8 Process Gas out through T-valve 24, SO in the Process Gas
2And H
2S low-temp reaction on beds generates elemental sulfur; Enter three grades of condensers 8 from second reactor 14 Process Gas out and be cooled to 125 ℃, sulfur vapor obtains condensation and separates; Enter sulphur mist trap 9 from three grades of condensers 7 Process Gas out through T-valve 23, after over cure mist trap 9 captured the sulphur mist that contains in the Process Gas, Process Gas passes into 19 calcinations of reclamation tail gas burning stove, and was emptying by chimney 20.
The below is in conjunction with Fig. 3, and the embodiment of this patent is described.As shown in Figure 3, the acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, are cooled to 315 ℃ from main burning furnace 1 pyroprocess gas out through waste heat boiler 2; Enter gas/gas interchanger 3 from waste heat boiler 2 Process Gas out, carry out heat exchange temperature with quench tower 10 exit procedure gas and be down to 272.3 ℃; Process Gas after heat exchange enters first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; Enter quench tower circulation device 5,10 from first-stage condenser 4 Process Gas out, Process Gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is on a small quantity state of saturation is then all sublimated and is solid-state sulphur; Carry out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas from quench tower 10 Process Gas out, temperature is increased to 100 ℃; Process Gas enters the online roasting kiln 11 of one-level after the preheating, and temperature rises to 220 ℃; Enter one-level catalytic converter 12, SO from the online roasting kiln 11 of one-level Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter secondary condenser 6 from one-level catalytic converter 12 Process Gas out and be cooled to 173 ℃, sulfur vapor obtains condensation and separates; Enter the online roasting kiln 13 of secondary from secondary condenser 6 Process Gas out, temperature rises to 204 ℃; Enter secondary catalytic converter 14, SO from the online roasting kiln 13 of secondary Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter three grades of condensers 7 from secondary catalytic converter 14 Process Gas out and be cooled to 162 ℃, sulfur vapor obtains condensation and separates; Enter three grades of online roasting kilns 15 from three grades of condensers 7 Process Gas out, temperature rises to 198 ℃; Enter three grades of catalytic converters 16, SO from three grades of online roasting kilns 15 Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter level Four condenser 8 from three grades of catalytic converters 16 Process Gas out and be cooled to 162 ℃, sulfur vapor obtains condensation and separates; Enter the online roasting kiln 17 of level Four from level Four condenser 8 Process Gas out, temperature rises to about 320 ℃; Enter hydrogenator 28 from the online roasting kiln 17 of level Four Process Gas out, sulfocompound residual in the Process Gas is reduced to H
2S; Enter quench tower 25 from hydrogenator 28 Process Gas out, Process Gas is cooled in quench tower, enters absorption tower 26 from quench tower 25 Process Gas out, the H in the Process Gas
2S is absorbed in absorption tower 26; Self-absorption tower 26 out contain H
2The S solution H that in regenerator column 27, regenerates
2S again enters recovery technique and processes; Self-absorption tower 26 Process Gas out then directly passes into 19 calcinations of reclamation tail gas burning stove, and is emptying by chimney 20.
The below is in conjunction with Fig. 4, and the embodiment of this patent is described.As shown in Figure 4, the acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, are cooled to 315 ℃ from main burning furnace 1 pyroprocess gas out through waste heat boiler 2; Enter gas/gas interchanger 3 from waste heat boiler 2 Process Gas out, carry out heat exchange temperature with quench tower 10 exit procedure gas and be down to 272.3 ℃; Process Gas after heat exchange enters first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; Enter quench tower circulation device 5,10 from first-stage condenser 4 Process Gas out, Process Gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is on a small quantity state of saturation is then all sublimated and is solid-state sulphur; Carry out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas from quench tower 10 Process Gas out, temperature is increased to 100 ℃; Process Gas enters the online roasting kiln 11 of one-level after the preheating, and temperature rises to 220 ℃; Enter one-level catalytic converter 12, SO from the online roasting kiln 11 of one-level Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter secondary condenser 6 from one-level catalytic converter 12 Process Gas out and be cooled to 173 ℃, sulfur vapor obtains condensation and separates; Enter the online roasting kiln 13 of secondary from secondary condenser 6 Process Gas out, temperature rises to 204 ℃; Enter secondary catalytic converter 14, SO from the online roasting kiln 13 of secondary Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter three grades of condensers 7 from secondary catalytic converter 14 Process Gas out and be cooled to 162 ℃, sulfur vapor obtains condensation and separates; Enter three grades of online roasting kilns 15 from three grades of condensers 7 Process Gas out, temperature rises to 198 ℃; Enter three grades of catalytic converters 16, SO from three grades of online roasting kilns 15 Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter level Four condenser 8 from three grades of catalytic converters 16 Process Gas out and be cooled to 126 ℃, sulfur vapor obtains condensation and separates; Enter sulphur mist trap 9 from level Four condenser 8 Process Gas out, after over cure mist trap 9 captured the sulphur mist that contains in the Process Gas, Process Gas passes into 19 calcinations of reclamation tail gas burning stove, and was emptying by chimney 20.
The below is in conjunction with Fig. 5, and the embodiment of this patent is described.As shown in Figure 5, the acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, are cooled to 315 ℃ from main burning furnace 1 pyroprocess gas out through waste heat boiler 2; Enter gas/gas interchanger 3 from waste heat boiler 2 Process Gas out, carry out heat exchange temperature with quench tower 10 exit procedure gas and be down to 272.3 ℃; Process Gas after heat exchange enters first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; Enter quench tower circulation device 5,10 from first-stage condenser 4 Process Gas out, Process Gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is on a small quantity state of saturation is then all sublimated and is solid-state sulphur; Carry out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas from quench tower 10 Process Gas out, temperature is increased to 100 ℃; Process Gas enters the online roasting kiln 11 of one-level after the preheating, and temperature rises to 220 ℃; Enter one-level catalytic converter 12, SO from the online roasting kiln 11 of one-level Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter secondary condenser 6 from one-level catalytic converter 12 Process Gas out and be cooled to 173 ℃, sulfur vapor obtains condensation and separates; Enter the online roasting kiln 13 of secondary from secondary condenser 6 Process Gas out, temperature rises to 204 ℃; Enter secondary catalytic converter 14, SO from the online roasting kiln 13 of secondary Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter three grades of condensers 7 from secondary catalytic converter 14 Process Gas out and be cooled to 162 ℃, sulfur vapor obtains condensation and separates; Enter sulphur mist trap 9 from three grades of condensers 7 Process Gas out, after over cure mist trap 9 captured the sulphur mist that contains in the Process Gas, Process Gas passes into 19 calcinations of reclamation tail gas burning stove, and was emptying by chimney 20.
Claims (1)
1. type sulfur recovery method that dewaters, it is characterized in that: processing step is as follows:
The first step: the acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln, and out pyroprocess gas is cooled to 315 ℃ through waste heat boiler in main burning furnace; Enter gas/gas interchanger from waste heat boiler Process Gas out, carry out heat exchange temperature with quench tower exit procedure gas and be down to 272.3 ℃;
Second step: the Process Gas after heat exchange enters first-stage condenser and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; Enter the quench tower circulation device from first-stage condenser Process Gas out, Process Gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is on a small quantity state of saturation is all sublimated and is solid-state sulphur;
The 3rd step: carry out heat exchange from quench tower Process Gas out through gas/gas interchanger and waste heat boiler exit procedure gas, temperature is increased to 100 ℃; Process Gas after the preheating enters the online roasting kiln of one-level; Enter one-level catalytic converter, SO from the online roasting kiln of one-level Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter the secondary condenser cooling from one-level catalytic converter Process Gas out, sulfur vapor obtains condensation and separates;
The 4th step: enter the online roasting kiln of secondary from secondary condenser Process Gas out; Enter secondary catalytic converter, SO from the online roasting kiln of secondary Process Gas out
2And H
2S generates elemental sulfur in the beds reaction; Enter three grades of condenser coolings from secondary catalytic converter Process Gas out, sulfur vapor obtains condensation and separates;
The 5th step: enter three grades of online roasting kilns from three grades of condensers Process Gas out; Enter the online roasting kiln of level Four from three grades of catalytic converters Process Gas out and an amount of air proportioning; Enter the direct oxidation reactor, the H in the Process Gas from the online roasting kiln of level Four Process Gas out
2The direct oxidation under the effect of catalyzer of S gas is elemental sulfur; Enter last condenser stage from direct oxidation reactor gas out, sulfur vapor obtains condensation and separates;
The device of the described type sulfur recovery method that dewaters is:
By main burning furnace, waste heat boiler, gas/gas interchanger, condenser, for water circle device, sulphur mist trap, quench tower, online roasting kiln, convertor, super Crouse's convertor, the reclamation tail gas burning stove, chimney consists of; Main burning furnace and waste heat boiler join end to end, and the waste heat boiler outlet is connected with gas/gas heat exchanger tube pass entrance, and gas/gas heat exchanger tube pass outlet is connected with the first-stage condenser entrance; The first-stage condenser outlet is connected with the quench tower bottom inlet; Entrance for water circle device is connected with the outlet at bottom of quench tower, supplies the outlet of water circle device to be connected with the upper side entrance of quench tower, and connection line is provided with the magnetic valve that is connected with the water-content supervisory system with temperature; The top exit of quench tower is connected with the shell side entrance of gas/gas interchanger, and connection line is provided with temperature and crosses and the water-content supervisory system; The shell side outlet of gas/gas interchanger is connected with the online roasting kiln of one-level.
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| CN103159187B (en) * | 2013-03-27 | 2014-08-13 | 山东三维石化工程股份有限公司 | Shutdown technique of cleaner production of sulfur recovery and tail gas treatment device |
| CN103964399B (en) * | 2014-05-07 | 2015-07-15 | 中国石油集团工程设计有限责任公司 | Sulfur recovering heat utilization device and method |
| CN106586973B (en) * | 2016-11-30 | 2018-11-02 | 成都丽雅纤维股份有限公司 | A method of being used for Crouse's direct current method Recovered sulphur |
| RU2639701C1 (en) * | 2017-03-03 | 2017-12-21 | Акционерное общество "Гипрогазоочистка" | Method for disposal of acid gases containing hydrogen sulphide and ammonia according to claus method below dew point |
| CN106955595B (en) * | 2017-04-19 | 2020-03-20 | 成都天立化工科技有限公司 | Regeneration method of desulfurizer elemental sulfur in desulfurizing tower |
| CN113912022B (en) * | 2020-07-10 | 2023-06-23 | 宝武碳业科技股份有限公司 | SO in process gas at outlet of combustion furnace of sulfuric acid lifting device 2 Concentration process |
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| GB0015984D0 (en) * | 2000-06-29 | 2000-08-23 | Boc Group Plc | Treatment of feed gas streams containing hydrogen sulphide |
| CN1213791C (en) * | 2000-09-07 | 2005-08-10 | 英国氧气集团有限公司 | Process and apparatus for recovering sulphur from gas stream containing hydrogen sulphide |
| CN101927982B (en) * | 2010-08-27 | 2011-11-16 | 西南石油大学 | Isothermal direct oxidization recovery technology of sulfur |
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