CN102530882A - Method and device for reclaiming dehydrated sulfur - Google Patents
Method and device for reclaiming dehydrated sulfur Download PDFInfo
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- CN102530882A CN102530882A CN2010106164312A CN201010616431A CN102530882A CN 102530882 A CN102530882 A CN 102530882A CN 2010106164312 A CN2010106164312 A CN 2010106164312A CN 201010616431 A CN201010616431 A CN 201010616431A CN 102530882 A CN102530882 A CN 102530882A
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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 and handle 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 sulier from Sweet natural gas and refinery gas, minimizing SO
2The sulfur recovery and the tail gas treatment process of quantity discharged have obtained tremendous development.In simple terms; Having with CBA, MCRC, Clinsulf-SDP, Sulfreen and Clauspol etc. is the inferior dew point technology of representative; With Clinsulf-DO, ENsulf, Selectox, Superclaus and Modop etc. is the direct oxidation technology of representative, is the oxygen enriching process of representative and is the reduction absorption technique of representative with SCOT, BSRP, LTGT, Resulf and RAR etc. with Oxyclaus, Sure and COPE etc.Also having with Wellman-Lord technology and Cansolv technology in addition is the oxidation absorption technique of representative, because technical process is comparatively complicated, equipment corrosion is comparatively serious, uses few.
From present applicable cases, use maximum be the reduction absorption technique, secondly be inferior dew point technology, be direct oxidation technology once more, be oxygen enriching process at last.The oxidation absorption technique is not almost seen formal industrial application report.In general, contain a large amount of water vapour and be in the sulfur vapor under the state of saturation on a small quantity in the Cross unit process gas usually.The two is as the resultant of claus reaction, and the high more claus reaction sulphur of its concentration transformation efficiency is more little.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 air water vapor content at different levels constantly increase.The process air water vapor content that goes out the last step reactor drum in typical case is usually up to 20～30%.Receive the restriction of Crouse's balanced reaction, the total sulphur recovery of technology has received influence 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 process gas preheating 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, removes water section, heat, regenerator section and catalytic conversion part again.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 gets into quench tower and is cooled to lesser temps; A large amount of water vapor condensations are liquid water in the process gas; Be in sulfur vapor under the state of saturation on a small quantity 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 helps generating sulphur in the downstream unit.Quench tower exit procedure gas gets into 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 takes place in downstream unit, and the content of water vapour and sulfur vapor obtains reducing in the one-level convertor entry process gas, and downstream unit sulphur transformation efficiency is improved.
Method steps is described below: acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln, and the pyroprocess gas that in main burning furnace, comes out is cooled to 315 ℃ through waste heat boiler; The process gas that comes out from waste heat boiler gets into gas/gas interchanger, carries out heat exchange temperature with quench tower exit procedure gas and reduces to 272.3 ℃; Process gas after heat exchange gets into first-stage condenser and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from first-stage condenser gets into the quench tower circulation device, and process gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is in state of saturation is on a small quantity all sublimated and is solid-state sulphur; The process gas that comes out from quench tower carries out heat exchange through gas/gas interchanger and waste heat boiler exit procedure gas, and temperature is increased to 100 ℃; Process gas after the preheating gets into the online roasting kiln of one-level; The process gas that comes out from the online roasting kiln of one-level gets into one-level catalytic converter, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas that comes out from the one-level catalytic converter gets into the secondary condenser cooling, and sulfur vapor obtains condensation and separates; The process gas that comes out from secondary condenser gets into the online roasting kiln of secondary; The process gas that comes out from the online roasting kiln of secondary gets into secondary catalytic converter, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas that comes out from the secondary catalytic converter gets into three grades of condensing surface coolings, and sulfur vapor obtains condensation and separates; The process gas that comes out from three grades of condensing surfaces gets into three grades of online roasting kilns; The process gas that comes out from three grades of catalytic converters gets into the online roasting kiln of level Four with an amount of air proportioning; The process gas that comes out from the online roasting kiln of level Four gets into direct oxidation reactor drum, the H in the process gas
2The direct oxidation under the effect of catalyzer of S gas is an elemental sulfur; The gas that comes out from the direct oxidation reactor drum gets into last condenser stage, and sulfur vapor obtains condensation and separates.The direct oxidation catalyzer is for being carrier with silicon-dioxide, and red stone is an active ingredient; The used catalyzer of catalytic converter is conventional activated alumina catalyst.
The present invention has following advantage:
1, the present invention is provided with earlier a cover quench tower device after first-stage condenser, and process temperature degree is reduced to 35～60 ℃, and making its a large amount of water vapor condensations that contain is liquid water, and the sulfur vapor that is in state of saturation is on a small quantity sublimated and is solid-state sulphur.Make downstream Cross unit sulfur conversion rate improve because of the water vapour that contains and sulfur vapor reduce in the process gas, and then increased the total sulphur recovery of technology.
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 water supply circulation devices; 6 secondary condensers, 7 three grades of condensing surfaces, 8 level Four condensing surfaces, 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 tail gas incinerators, 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 water supply circulation devices; 6 secondary condensers, 7 three grades of condensing surfaces, 8 level Four condensing surfaces, 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 tail gas incinerators; 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 water supply circulation devices, 6 secondary condensers; 7 three grades of condensing surfaces, 8 level Four condensing surfaces, 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 tail gas incinerators; 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 water supply circulation devices; 6 secondary condensers, 7 three grades of condensing surfaces, 8 level Four condensing surfaces, 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 tail gas incinerators, 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 water supply circulation devices, 6 secondary condensers, 7 three grades of condensing surfaces, 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 tail gas incinerators, 20 chimneys.
Fig. 6 is for quench tower dewaters, sulphur removal recycle system synoptic diagram.
Shown in Figure 6: 1 main burning furnace, 2 waste heat boilers, 3 gas/gas interchanger, 4 first-stage condenser, 5 water supply circulation devices, 10 quench towers, the online roasting kiln of 11 one-levels, 29 temperature are crossed and the water-content supervisory system, 30 SVs.
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, condensing surface; Water supply circulation device 5, sulphur mist trap 9, quench tower 10, online roasting kiln; Convertor, super Crouse's convertor 18, tail gas incinerator 19, chimney 20 constitutes; Main burning furnace 1 joins end to end with waste heat boiler 2, and waste heat boiler 2 outlets are connected with gas/gas interchanger 3 tube sides inlet, and gas/gas interchanger 3 tube sides outlet is connected with first-stage condenser 4 inlets; First-stage condenser 4 outlets are connected with quench tower 10 bottom inlets; The inlet of water supply circulation device 5 is connected with the outlet at bottom of quench tower 10, and the outlet of water supply circulation device 5 is connected with the last side entrance of quench tower 10, and connection line is provided with temperature and crosses the SV 30 that is connected with water-content supervisory system 29; The top exit of quench tower 10 is connected with the shell side inlet 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 that constitutes by convertor, condensing surface, online roasting kiln, sulphur mist trap 9, tail gas incinerator 19, chimney 20 connects.
Be to combine Fig. 1 below, the embodiment of this patent is described.Shown in accompanying drawing 1, acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, and the pyroprocess gas that comes out from main burning furnace 1 is cooled to 315 ℃ through waste heat boiler 2; The process gas that comes out from waste heat boiler 2 gets into gas/gas interchanger 3, carries out heat exchange temperature with quench tower 10 exit procedure gas and reduces to 272.3 ℃; Process gas after heat exchange gets into first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from first-stage condenser 4 gets into quench tower circulation device 5,10, and process gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is in state of saturation is on a small quantity then all sublimated and is solid-state sulphur; The process gas that comes out from quench tower 10 carries out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas, and temperature is increased to 100 ℃; Process gas gets into the online roasting kiln 11 of one-level after the preheating, and temperature rises to 220 ℃; The process gas that comes out from the online roasting kiln 11 of one-level gets into one-level catalytic converter 12, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas entering secondary condenser 6 that comes out from one-level catalytic converter 12 is cooled to 173 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from secondary condenser 6 gets into the online roasting kiln 13 of secondary, and temperature rises to 204 ℃; The process gas that comes out from the online roasting kiln 13 of secondary gets into secondary catalytic converter 14, SO
2And H
2S reacts on beds and generates elemental sulfur; The three grades of condensing surfaces 7 of process gas entering that come out from secondary catalytic converter 14 are cooled to 162 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from three grades of condensing surfaces 7 gets into three grades of online roasting kilns 15, and temperature rises to 220 ℃; The process gas that comes out from three grades of catalytic converters 16 gets into the online roasting kiln 17 of level Four with an amount of air proportioning, and temperature rises to 210 ℃; The process gas that comes out from the online roasting kiln 17 of level Four gets into super Crouse's convertor 18, the H in the process gas
2The direct oxidation under the effect of catalyzer of S gas is an elemental sulfur; The gas that comes out from super Crouse's convertor 18 gets into last condenser stage 8, and 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 fed 19 calcinations of tail gas incinerator, through chimney 20 emptyings.
Be to combine Fig. 2 below, the embodiment of this patent is described.Shown in accompanying drawing 2, acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, and the pyroprocess gas that comes out from main burning furnace 1 is cooled to 315 ℃ through waste heat boiler 2; The process gas that comes out from waste heat boiler 2 gets into gas/gas interchanger 3, carries out heat exchange temperature with quench tower 10 exit procedure gas and reduces to 272.3 ℃; Process gas after heat exchange gets into first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from first-stage condenser 4 gets into quench tower circulation device 5,10, and process gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is in state of saturation is on a small quantity then all sublimated and is solid-state sulphur; The process gas that comes out from quench tower 10 carries out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas, and temperature is increased to 100 ℃; Process gas gets into the online roasting kiln 11 of one-level after the preheating, and temperature rises to 279 ℃; The process gas that comes out from the online roasting kiln 11 of one-level gets into one-level catalytic converter 12, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas that comes out from one-level catalytic converter 12 gets into gas/gas interchanger 21 tube sides, and tube side exit procedure gas gets into secondary condenser 6 and is cooled to 173 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from secondary condenser 6 gets into gas/gas interchanger 21 shell sides, and shell side exit procedure gas gets into second reactor 14 through T-valve 22, and catalyzer is regenerated, simultaneously SO
2And H
2S reacts on beds and generates elemental sulfur; The three grades of condensing surfaces 7 of process gas entering that come out from second reactor are cooled to 126 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from three grades of condensing surfaces 7 gets into three reactor 16, SO in the process gas through T-valve 23
2And H
2S low-temp reaction on beds generates elemental sulfur; The process gas entering level Four condensing surface 8 that comes out from three reactor 16 is cooled to 125 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from level Four condensing surface 8 gets into sulphur mist trap 9 through T-valve 24, and after over cure mist trap 9 captured the sulphur mist that contains in the process gas, process gas fed 19 calcinations of tail gas incinerator, through chimney 20 emptyings.
Switch: after the switching, gas/gas interchanger 21 shell sides are made a slip of the tongue journey gas through T-valve 22 entering three reactors 16 certainly, and catalyzer is regenerated, simultaneously SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas entering level Four condensing surface 8 that comes out from three reactor 16 is cooled to 126 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from level Four condensing surface 8 gets into second reactor 14, SO in the process gas through T-valve 24
2And H
2S low-temp reaction on beds generates elemental sulfur; The three grades of condensing surfaces 8 of process gas entering that come out from second reactor 14 are cooled to 125 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from three grades of condensing surfaces 7 gets into sulphur mist trap 9 through T-valve 23, and after over cure mist trap 9 captured the sulphur mist that contains in the process gas, process gas fed 19 calcinations of tail gas incinerator, through chimney 20 emptyings.
Be to combine Fig. 3 below, the embodiment of this patent is described.Shown in accompanying drawing 3, acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, and the pyroprocess gas that comes out from main burning furnace 1 is cooled to 315 ℃ through waste heat boiler 2; The process gas that comes out from waste heat boiler 2 gets into gas/gas interchanger 3, carries out heat exchange temperature with quench tower 10 exit procedure gas and reduces to 272.3 ℃; Process gas after heat exchange gets into first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from first-stage condenser 4 gets into quench tower circulation device 5,10, and process gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is in state of saturation is on a small quantity then all sublimated and is solid-state sulphur; The process gas that comes out from quench tower 10 carries out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas, and temperature is increased to 100 ℃; Process gas gets into the online roasting kiln 11 of one-level after the preheating, and temperature rises to 220 ℃; The process gas that comes out from the online roasting kiln 11 of one-level gets into one-level catalytic converter 12, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas entering secondary condenser 6 that comes out from one-level catalytic converter 12 is cooled to 173 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from secondary condenser 6 gets into the online roasting kiln 13 of secondary, and temperature rises to 204 ℃; The process gas that comes out from the online roasting kiln 13 of secondary gets into secondary catalytic converter 14, SO
2And H
2S reacts on beds and generates elemental sulfur; The three grades of condensing surfaces 7 of process gas entering that come out from secondary catalytic converter 14 are cooled to 162 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from three grades of condensing surfaces 7 gets into three grades of online roasting kilns 15, and temperature rises to 198 ℃; The process gas that comes out from three grades of online roasting kilns 15 gets into three grades of catalytic converters 16, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas entering level Four condensing surface 8 that comes out from three grades of catalytic converters 16 is cooled to 162 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from level Four condensing surface 8 gets into the online roasting kiln 17 of level Four, and temperature rises to about 320 ℃; The process gas that comes out from the online roasting kiln 17 of level Four gets into hydrogenator 28, and sulfocompound residual in the process gas is reduced to H
2S; The process gas that comes out from hydrogenator 28 gets into quench tower 25, and process gas is cooled in quench tower, and the process gas that comes out from quench tower 25 gets into absorption tower 26, the H in the process gas
2S is absorbed in absorption tower 26; Self-absorption tower 26 comes out contains H
2The S solution H that in regenerator column 27, regenerates
2S gets into recovery technology once more and handles; The process gas that self-absorption tower 26 comes out then directly feeds 19 calcinations of tail gas incinerator, through chimney 20 emptyings.
Be to combine Fig. 4 below, the embodiment of this patent is described.Shown in accompanying drawing 4, acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, and the pyroprocess gas that comes out from main burning furnace 1 is cooled to 315 ℃ through waste heat boiler 2; The process gas that comes out from waste heat boiler 2 gets into gas/gas interchanger 3, carries out heat exchange temperature with quench tower 10 exit procedure gas and reduces to 272.3 ℃; Process gas after heat exchange gets into first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from first-stage condenser 4 gets into quench tower circulation device 5,10, and process gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is in state of saturation is on a small quantity then all sublimated and is solid-state sulphur; The process gas that comes out from quench tower 10 carries out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas, and temperature is increased to 100 ℃; Process gas gets into the online roasting kiln 11 of one-level after the preheating, and temperature rises to 220 ℃; The process gas that comes out from the online roasting kiln 11 of one-level gets into one-level catalytic converter 12, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas entering secondary condenser 6 that comes out from one-level catalytic converter 12 is cooled to 173 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from secondary condenser 6 gets into the online roasting kiln 13 of secondary, and temperature rises to 204 ℃; The process gas that comes out from the online roasting kiln 13 of secondary gets into secondary catalytic converter 14, SO
2And H
2S reacts on beds and generates elemental sulfur; The three grades of condensing surfaces 7 of process gas entering that come out from secondary catalytic converter 14 are cooled to 162 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from three grades of condensing surfaces 7 gets into three grades of online roasting kilns 15, and temperature rises to 198 ℃; The process gas that comes out from three grades of online roasting kilns 15 gets into three grades of catalytic converters 16, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas entering level Four condensing surface 8 that comes out from three grades of catalytic converters 16 is cooled to 126 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from level Four condensing surface 8 gets into sulphur mist trap 9, and after over cure mist trap 9 captured the sulphur mist that contains in the process gas, process gas fed 19 calcinations of tail gas incinerator, through chimney 20 emptyings.
Be to combine Fig. 5 below, the embodiment of this patent is described.Shown in accompanying drawing 5, acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln 1, and the pyroprocess gas that comes out from main burning furnace 1 is cooled to 315 ℃ through waste heat boiler 2; The process gas that comes out from waste heat boiler 2 gets into gas/gas interchanger 3, carries out heat exchange temperature with quench tower 10 exit procedure gas and reduces to 272.3 ℃; Process gas after heat exchange gets into first-stage condenser 4 and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from first-stage condenser 4 gets into quench tower circulation device 5,10, and process gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is in state of saturation is on a small quantity then all sublimated and is solid-state sulphur; The process gas that comes out from quench tower 10 carries out heat exchange through gas/gas interchanger 3 with waste heat boiler 2 exit procedure gas, and temperature is increased to 100 ℃; Process gas gets into the online roasting kiln 11 of one-level after the preheating, and temperature rises to 220 ℃; The process gas that comes out from the online roasting kiln 11 of one-level gets into one-level catalytic converter 12, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas entering secondary condenser 6 that comes out from one-level catalytic converter 12 is cooled to 173 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from secondary condenser 6 gets into the online roasting kiln 13 of secondary, and temperature rises to 204 ℃; The process gas that comes out from the online roasting kiln 13 of secondary gets into secondary catalytic converter 14, SO
2And H
2S reacts on beds and generates elemental sulfur; The three grades of condensing surfaces 7 of process gas entering that come out from secondary catalytic converter 14 are cooled to 162 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from three grades of condensing surfaces 7 gets into sulphur mist trap 9, and after over cure mist trap 9 captured the sulphur mist that contains in the process gas, process gas fed 19 calcinations of tail gas incinerator, through chimney 20 emptyings.
Claims (2)
1. type sulfur recovery method that dewaters, it is characterized in that: process step is following:
The first step: acid gas after the preheating and air carry out claus reaction by certain proportioning in roasting kiln, and the pyroprocess gas that in main burning furnace, comes out is cooled to 315 ℃ through waste heat boiler; The process gas that comes out from waste heat boiler gets into gas/gas interchanger, carries out heat exchange temperature with quench tower exit procedure gas and reduces to 272.3 ℃;
Second step: the process gas after heat exchange gets into first-stage condenser and is cooled to 164 ℃, and sulfur vapor obtains condensation and separates; The process gas that comes out from first-stage condenser gets into the quench tower circulation device, and process gas is cooled to 35～60 ℃, and wherein most water vapor condensations are molten sulfur, and the sulfur vapor that is in state of saturation is on a small quantity all sublimated and is solid-state sulphur;
The 3rd step: the process gas that comes out from quench tower carries out heat exchange through gas/gas interchanger and waste heat boiler exit procedure gas, and temperature is increased to 100 ℃; Process gas after the preheating gets into the online roasting kiln of one-level; The process gas that comes out from the online roasting kiln of one-level gets into one-level catalytic converter, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas that comes out from the one-level catalytic converter gets into the secondary condenser cooling, and sulfur vapor obtains condensation and separates;
The 4th step: the process gas that comes out from secondary condenser gets into the online roasting kiln of secondary; The process gas that comes out from the online roasting kiln of secondary gets into secondary catalytic converter, SO
2And H
2S reacts on beds and generates elemental sulfur; The process gas that comes out from the secondary catalytic converter gets into three grades of condensing surface coolings, and sulfur vapor obtains condensation and separates;
The 5th step: the process gas that comes out from three grades of condensing surfaces gets into three grades of online roasting kilns; The process gas that comes out from three grades of catalytic converters gets into the online roasting kiln of level Four with an amount of air proportioning; The process gas that comes out from the online roasting kiln of level Four gets into direct oxidation reactor drum, the H in the process gas
2The direct oxidation under the effect of catalyzer of S gas is an elemental sulfur; The gas that comes out from the direct oxidation reactor drum gets into last condenser stage, and sulfur vapor obtains condensation and separates.
2. described type sulfur recovery facility that dewaters of claim 1, by main burning furnace, waste heat boiler, gas/gas interchanger, condensing surface; The water supply circulation device, sulphur mist trap, quench tower, online roasting kiln; Convertor, super Crouse's convertor, the tail gas incinerator, chimney constitutes; It is characterized in that: main burning furnace and waste heat boiler join end to end, and the waste heat boiler outlet is connected with gas/gas interchanger tube side inlet, and gas/gas interchanger tube side outlet is connected with the first-stage condenser inlet; The first-stage condenser outlet is connected with the quench tower bottom inlet; The inlet of water supply circulation device is connected with the outlet at bottom of quench tower, and the outlet of water supply circulation device is connected with the last side entrance of quench tower, and connection line is provided with temperature and crosses the SV that is connected with the water-content supervisory system; The top exit of quench tower is connected with the shell side inlet 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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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103159187A (en) * | 2013-03-27 | 2013-06-19 | 山东三维石化工程股份有限公司青岛分公司 | Shutdown technique of cleaner production of sulfur recovery and tail gas treatment device |
| CN103964399A (en) * | 2014-05-07 | 2014-08-06 | 中国石油集团工程设计有限责任公司 | Sulfur recovering heat utilization device and method |
| CN106586973A (en) * | 2016-11-30 | 2017-04-26 | 成都丽雅纤维股份有限公司 | Method for recycling sulphur through Claus direct-current process |
| CN106955595A (en) * | 2017-04-19 | 2017-07-18 | 成都天立化工科技有限公司 | The renovation process of desulfurizing agent simple substance sulphur in a kind of desulfurizing tower |
| 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 |
| CN113912022A (en) * | 2020-07-10 | 2022-01-11 | 宝武炭材料科技有限公司 | SO in process gas at outlet of combustion furnace of sulfuric acid lifting device2Concentration process |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103159187A (en) * | 2013-03-27 | 2013-06-19 | 山东三维石化工程股份有限公司青岛分公司 | Shutdown technique of cleaner production of sulfur recovery and tail gas treatment device |
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| CN106586973A (en) * | 2016-11-30 | 2017-04-26 | 成都丽雅纤维股份有限公司 | Method for recycling sulphur through Claus direct-current process |
| 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 |
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| CN113912022A (en) * | 2020-07-10 | 2022-01-11 | 宝武炭材料科技有限公司 | SO in process gas at outlet of combustion furnace of sulfuric acid lifting device2Concentration process |
| 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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| CN102530882B (en) | 2013-10-16 |
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