CA2035554A1 - Method for the automatic control of the rate of supply of oxygen to a claus process plant - Google Patents
Method for the automatic control of the rate of supply of oxygen to a claus process plantInfo
- Publication number
- CA2035554A1 CA2035554A1 CA 2035554 CA2035554A CA2035554A1 CA 2035554 A1 CA2035554 A1 CA 2035554A1 CA 2035554 CA2035554 CA 2035554 CA 2035554 A CA2035554 A CA 2035554A CA 2035554 A1 CA2035554 A1 CA 2035554A1
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- Prior art keywords
- rate
- oxygen
- gas
- combustion chamber
- measured
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
- C01B17/0452—Process control; Start-up or cooling-down procedures of the Claus process
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
- C01B17/0413—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the combustion step
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Automation & Control Theory (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
Abstract
ABSTRACT
An H2S-containing feed gas is partly combusted with an oxygen-containing gas in a combustion chamber of a Claus process plant so that a gas mixture is formed which contains H2S and SO2, which are reacted to produce elementary sulfur. The gas mixture leaving the combustion chamber is reacted in one or more cata-lytic processing stages and optionally in aftertreating means. The concentrations of H2S and SO2 are measured upstream or downstream of one of the catalytic proces-sing states or upstream or downstream of the after-treating means or in such aftertreating means. The rate at which the feed gas enters the combustion chamber and the rate of supply of the oxygen-containing gas to the combustion chamber are also measured. A controller is used to calculate from the values thus measured the rate at which the oxygen-containing gas is to be supplied to the combustion chamber in order to minimize the content of sulfur compounds in the exhaust gas.
An H2S-containing feed gas is partly combusted with an oxygen-containing gas in a combustion chamber of a Claus process plant so that a gas mixture is formed which contains H2S and SO2, which are reacted to produce elementary sulfur. The gas mixture leaving the combustion chamber is reacted in one or more cata-lytic processing stages and optionally in aftertreating means. The concentrations of H2S and SO2 are measured upstream or downstream of one of the catalytic proces-sing states or upstream or downstream of the after-treating means or in such aftertreating means. The rate at which the feed gas enters the combustion chamber and the rate of supply of the oxygen-containing gas to the combustion chamber are also measured. A controller is used to calculate from the values thus measured the rate at which the oxygen-containing gas is to be supplied to the combustion chamber in order to minimize the content of sulfur compounds in the exhaust gas.
Description
.
55~
Metallgesellschaft AG February 209 1990 Reuterweg 14 6000 Frankfurt on-Main 1 Case No. 890030 Method for the Automatic Control of the Rate of Supply of Oxygen to a Claus ~'rocess Plan-t . .
DESCRI~ION
~his invention relates to a method for.-operatin~ a plant for producing elemen,tary sulfur in a process in which an H2s-containing feed gas i5 partly combusted with an oxygen-containin~ gas in a combustion ~ :
: chamber of a Claus process plant and a gas mixture that !~
oonta1ns H25 and S02 is~thus produced, from which elemen-tarD sulfur is produced by a reaction of H2S with S02 and : is separated, wherein the reactio~ of the gas mixture coming from the combustion chamber is effected in one or more catalytic processing ska~es and optionally in after- :.
....
treatinPi meansO .:
: In laus proce~s pl~nts~ a 6as which contains :
; H2S is converted in known manner -to a mixture of H2S and 2 gase~ by a partial combustion and eleme~tary sulfur ~: :
~ .
:
.
:
~ : ~ .,, :
; ' -2- 2 ~ 3 ~
is produced from that mixture in accordance with the simplified reaction equation 2 H2S + SO2 = 3 S ~ 2 H20. Details of the process have been described in Published German Application 34 15 722 and the corres-ponding U.S. Patent 4,632,819 and in Ullmanns Encyklopa-die der technischen Chemie, 4~h edition (1982), volume 21, on pages 8-26. The catalysts employed in th~ catalytic processing stages of the Claus process plant usually consist substantially of alumina or titanium dioxide.
The gas mixture coming from the Claus process plant is usually subjected to an aftertreatment by which the con-tents of sulfur compounds, particularly of H2S and SO2, in the gas mixture are decreased further. In known after-trea~ing processes, elementary sulfur is formed by the reaction of H2S with SO2 or 2 on catalysts which also consist substantially of A1203 or TiO~. The gas mixture obtained by the aftertreatment contains residual H2S and 52 in a total of about 500 to 1500 ppm. That gas may be combusted and then discharged into the atmosphere.
It is an object of the invention to effect an automatic control of the rate of supply of oxygen to the combustion chamber of the Claus process plant with sufficient accuracy and in a manner which is as simple as possible. In the process described first hereinbefore this is accomplished in accordance with the invention in that the concentrations K and P of H2S and SO2 in the ~as . , .
~mixture are measured upstream or downstream of one of the catalytic processing stages or upstream or downstream of the after-- - ~
2 ~ 3 ~
treating means or in such aftertreating meansi, the rate of feed ga~ flowin~ to the combustion chamber and the rate of supply of the oxygen-contâinin., ~,~s to the com-bustion chamber ~re me~suredt the results of said measurements are indicated -to a controller and u~ed to calculate the correction rate by which the rate of oxy-gen-ccntaining gas must be corrected ~o adjust the dif erence D- ~ - a -~ P to zero, ~,vherein a is !~ factor that is specific to the process and lies between 0.1 and 10, and the rate of supply of oxygen-containing gas !;
to the co~bustion ~hamber is changed by the correction rateO : ' ~ ccordi~g to a further feature of the invention the stream OI~ oxygen-contair.ing gaS supplied to the combustion chamber is formed from a main stream and a supplemen~al stream, the rates of the main stream and of the supplemental stream are au~cmatically con- ~ :
trolled in dependence on the measurement of the rate of the feed gas~ and the xa-te of the supplemsntal stream is increased or decreased by the calculated correction rateO
~he correction rate L (in sm3/h, ~here :
sm3 is standard cubic meter) of the oxygen-containing gas is preferably calculated in a¢cordance with the formula :~
~' . , .
. ' 5 ~
wherein V = a factor that is speclfic to the process ~nd lies between 0~01 and 2.0, D = the concentra-tion diffelence ~L ~ a x P, me~sured in mole percent, E = rate of feed ~as measured in sm~/h, = percentage (in mole percent) of oxygen in the oxygen containing ~as, M = total rate (measured in sm3/h) of supply of the oxygen-containing gas to the combustion chamber.
The factor a which is specific to the process and i~uded in tne difference ~ = I`L ~ a x P
is determined by the desired ratio a = K/P of ths concen-. .
trations o~ H2S and S02 in the gas flowin~ through the ;~analyzer for mea~urlng~the concentrations, i.e~, bythat value o~ that ratlo which is regarded as an optimum.
AS a result, the fq~r a will depend on the ~reatment which succeeds the conce~tration measurement. If it is deslred to react H28 a~d S02 bv the reaction S02 ~
~ H2S to elementary sulfur also after the concentration a~nalysis5 a~will be 2~ The fa~tor V whLch is speci~7ic to the~process i~ determined by ~ trial operation of the plantO If the oxggen-con~aining gas ;Fed to the combustion hamber oons~i9t8 of pure air, S will be 21. If pure ` oxygen is used~or the combustion in the combustion chamber, S will be lO0.
, : : :
:: :
. 2~35~4 Detail~ of the automatic control in ac-cordance with the invention ~i.ll be ex~ained with reference to the illustrative embodiment of the process shown on the drawing~
The H2S-containing feed gas which is to be desulfurized is ~ed in line 1 to the combustion chamber 2 of a alaus process plantO Oxygen-containing gas is supplièd in line 3. '~he Claus process plant usu-ally comprises a plurallty of catalytic processi~g sta-ges, in which elementary sulfur is produced in accord- -.
ance with the (simplified) reaction equation 2 H2S ~
S2 = 3 S + 2 H20 from the gas mixture coming in line 4 from the combustion chamber 2. ~he sulfur i9 separated in a known manner, whlch is not shown hereO The drawing shows two catalytic ~rocessin~ stages 5 and 60 Part o~
the~elemen-tary sulfur Qay have been separated before the .`
catalytic stages by condensation from the gas mi~tuxe .. `:
coming from the combustion chamber 2. That ~as mixture flows -through the catalytlc processing stages 5 and 6 and then flows in line 7 to an analyzer 8, ~Jhich is incor- ` :
, porated in a branch line 7aO
he analyzer 8 detects the concentrations K and P of H2S and SO2 in the arrivi~ gas mixture, which :
is subseque~tly fed to the aftertreating means 9. In the aftertreating means the content o~ sulfur compounds in : ~: the~6as mixture is further decreased. The aftertreatment .
2 L3 3 ~
is not required in all cases and may be effected in known manner and in a plur~lity of parts or in a plula-lity of stages. The gas mixture is subsequently passed through afterburning means and is then discharged through a chimney 10 into the atmosphere.
il'he oxygen-containin~ ~as in line 3 is formed from a main stream supp~Lied in line 11 and of a supplemental stream supi)lied in line 12 and consisting of that ga;. ~he rates of said streams are cont~led by the flo~l control valves 1~ and 14. 'rO con-trol the rate of the maln stream in line 11, the rate of the feed gas in line 1 is measured b~ the flow meter ~
16 and -the rate signal is delivered via the signal line ~:
17 to a firs~ controller 18, w~lich acts on the flow oontrol valve 13 via the signal line 19. The same ra~e signal is delivered via à signal line 17a to a second controller 25 for adJusting the rate of the supplemental : stream of oxygen~containin; gas by means of the ~low c:ontrol valve 140 ~he flow meter 20 in line 11 indicates : ~ via the signal line 21 to the controller 18 the actual flow rate in line ll.
'l'he rate of the main stream of ~he oxygen-containing g~ fad to the combustion chamber 2 is ~::
co~trolled by means of the first controller 18. The secorld controller 25 serves also to e~ctly adjust the :~rate of supI)ly of oxygen to the combustion chamber 2 to - , :~ , ' ' '~:
: ~ "
2 ~ 5 ~7--the required value by a change of the rate of the supplementary s-tream comin from line 120 ~he control-ler 25 influences via the si~nal line 26 the flow control valve 14. In order -to determine the correction rate L by which the rate of the supplemental stream of oxygen~containing gas is to be chan~ed~ t~ correct- -ion rate ~ is calculated in the controller 25 i~ accord-ance with the formula ~ = D
S . .
The various parameters of said formula have been ex-plained hereinbefore. For the calculation of the cor-rection rate ~ the second controller 25 receives from the analyzer 8 via the signal li~e 8a the co~centration K of H2S and via the signal line 8~ the concen~ration -, . .~
P of S02 in the gas mixture which flo~ through -the anaIyzer. The -to~al rate ~i of oxygen-containing gas flowing in line 3 to the combustion chamber 2 is de-:~ ~te~mined by the meter 30 and the measured value is indi-cated via the signal line 31 to the controller 25, ~he flow meter 28 ln line 12 in~icates via the signal line 29~ to the oontroller 25 the rate at wbich oxygen-contain-ing g~s actually Elows through line 12 In a modification of the example illus-trated on the drawing the analy~er ~ :Eor measuring the ~ , concentrations of H2~ and S02 in the gas mixture may be ~arranged at different locations. ~he concentrations may ,, , ::, ~: : ' '' ~al3~
be analyzed upstream or do~vns-tream of any of ~he catalytic processin~ stages 5, 6 and upstr~am or downstream of a processin~ s~age which oelon~s to the aftertreatin~ means 9 or in such stage~ In -the embodi-ment of the process which is shown in the drawing the analyzer 8 is provided downstxeam of the last catalytic stage 6 of the Claus process I~lantO
.~xample In a processing s~stem as shown on the drawing, an H2S-containing feed ~a~ composed of H2S 7' mole ,'0 H2o 5.7 mole ,6 ~2 23.3 mole ~0 .
2H6 3r~0 mole ,~ -is fed at a rate of 8520~sm3/h to the combustion chamber 2 and is partly combusted therein with air supplied from~line 3 at a ra-te o~ 13793C:sm3/h. A main stream of th~ air is supplie:d at a rate of 12,510 sm3~h f~om : ~ . r : ~ : line 11 and a supplemental stream is supplied at a r~te of 1420 sm~/h from line 12. The Claus process plant con-tains arl A1203 catalyst in t~ro catal~tic sta~es 5 and 60 : Th~ analyzer 8 measures an H2S concentration I; of 0084 : mole percent: aDd an S0z concentratio~ P of 0.42 mole percentr. ~he desired value a:of the ratio K/~ is 2.00 ~: ~ '.' : ` ~
: ~ ; ~: :
., . . , . . . ..... , , - :: ; .: . . .
cj ,~
~ fter a ch~n~e of the concentratiion o~' H2S in the feed gas in J.ine 1 to 72 mole ~ercent, the ana-lyzer 8 will detect v.alues of E~ = 1049 mole percent and P - 0,32 mole percent. From a factor a = 2, S = 21 and a factor V = 0.412, which has been determined by a trial ::
operation, ~he controller 25 calculates the correction rate of air as ~ollows: ~
L = -Zl- (0.412 x 13,930 ~ 0.5 x 8520) = 404 sm3/h. ..
'~'' 3~ an adjustment of the flow control valve 14 the rate of air flowing in lines 12 and 3 is increased by that rate. .~s a result, an H2S concentration of 0~84 mole percent and an S02 concentration of 0~418 mole per-cent are rees~ablished in line 7 so that the desired ratio a = K~P = 2 is approxi~ated with ~ufficient accuracyD
The aftertreatment in 9 is pexformed by the Sulfreen ~rocess of Lurgi GmbH in Frankfurt on an A1203 catalyst by a re~ction of 2 H2S ~ S02 to 2 H2S +
3 SxO 600 p~m H2S and 300 ~rJm S02 are still found in the aft;ertreated gas. ~uel gas and air are added to~at gas, w~ich is then combusted and discharged into the atmos- .
phere O
, .
:: :
,~.', ; ' ,.';
~ ' . .
, . . . , ,, . " , ...
55~
Metallgesellschaft AG February 209 1990 Reuterweg 14 6000 Frankfurt on-Main 1 Case No. 890030 Method for the Automatic Control of the Rate of Supply of Oxygen to a Claus ~'rocess Plan-t . .
DESCRI~ION
~his invention relates to a method for.-operatin~ a plant for producing elemen,tary sulfur in a process in which an H2s-containing feed gas i5 partly combusted with an oxygen-containin~ gas in a combustion ~ :
: chamber of a Claus process plant and a gas mixture that !~
oonta1ns H25 and S02 is~thus produced, from which elemen-tarD sulfur is produced by a reaction of H2S with S02 and : is separated, wherein the reactio~ of the gas mixture coming from the combustion chamber is effected in one or more catalytic processing ska~es and optionally in after- :.
....
treatinPi meansO .:
: In laus proce~s pl~nts~ a 6as which contains :
; H2S is converted in known manner -to a mixture of H2S and 2 gase~ by a partial combustion and eleme~tary sulfur ~: :
~ .
:
.
:
~ : ~ .,, :
; ' -2- 2 ~ 3 ~
is produced from that mixture in accordance with the simplified reaction equation 2 H2S + SO2 = 3 S ~ 2 H20. Details of the process have been described in Published German Application 34 15 722 and the corres-ponding U.S. Patent 4,632,819 and in Ullmanns Encyklopa-die der technischen Chemie, 4~h edition (1982), volume 21, on pages 8-26. The catalysts employed in th~ catalytic processing stages of the Claus process plant usually consist substantially of alumina or titanium dioxide.
The gas mixture coming from the Claus process plant is usually subjected to an aftertreatment by which the con-tents of sulfur compounds, particularly of H2S and SO2, in the gas mixture are decreased further. In known after-trea~ing processes, elementary sulfur is formed by the reaction of H2S with SO2 or 2 on catalysts which also consist substantially of A1203 or TiO~. The gas mixture obtained by the aftertreatment contains residual H2S and 52 in a total of about 500 to 1500 ppm. That gas may be combusted and then discharged into the atmosphere.
It is an object of the invention to effect an automatic control of the rate of supply of oxygen to the combustion chamber of the Claus process plant with sufficient accuracy and in a manner which is as simple as possible. In the process described first hereinbefore this is accomplished in accordance with the invention in that the concentrations K and P of H2S and SO2 in the ~as . , .
~mixture are measured upstream or downstream of one of the catalytic processing stages or upstream or downstream of the after-- - ~
2 ~ 3 ~
treating means or in such aftertreating meansi, the rate of feed ga~ flowin~ to the combustion chamber and the rate of supply of the oxygen-contâinin., ~,~s to the com-bustion chamber ~re me~suredt the results of said measurements are indicated -to a controller and u~ed to calculate the correction rate by which the rate of oxy-gen-ccntaining gas must be corrected ~o adjust the dif erence D- ~ - a -~ P to zero, ~,vherein a is !~ factor that is specific to the process and lies between 0.1 and 10, and the rate of supply of oxygen-containing gas !;
to the co~bustion ~hamber is changed by the correction rateO : ' ~ ccordi~g to a further feature of the invention the stream OI~ oxygen-contair.ing gaS supplied to the combustion chamber is formed from a main stream and a supplemen~al stream, the rates of the main stream and of the supplemental stream are au~cmatically con- ~ :
trolled in dependence on the measurement of the rate of the feed gas~ and the xa-te of the supplemsntal stream is increased or decreased by the calculated correction rateO
~he correction rate L (in sm3/h, ~here :
sm3 is standard cubic meter) of the oxygen-containing gas is preferably calculated in a¢cordance with the formula :~
~' . , .
. ' 5 ~
wherein V = a factor that is speclfic to the process ~nd lies between 0~01 and 2.0, D = the concentra-tion diffelence ~L ~ a x P, me~sured in mole percent, E = rate of feed ~as measured in sm~/h, = percentage (in mole percent) of oxygen in the oxygen containing ~as, M = total rate (measured in sm3/h) of supply of the oxygen-containing gas to the combustion chamber.
The factor a which is specific to the process and i~uded in tne difference ~ = I`L ~ a x P
is determined by the desired ratio a = K/P of ths concen-. .
trations o~ H2S and S02 in the gas flowin~ through the ;~analyzer for mea~urlng~the concentrations, i.e~, bythat value o~ that ratlo which is regarded as an optimum.
AS a result, the fq~r a will depend on the ~reatment which succeeds the conce~tration measurement. If it is deslred to react H28 a~d S02 bv the reaction S02 ~
~ H2S to elementary sulfur also after the concentration a~nalysis5 a~will be 2~ The fa~tor V whLch is speci~7ic to the~process i~ determined by ~ trial operation of the plantO If the oxggen-con~aining gas ;Fed to the combustion hamber oons~i9t8 of pure air, S will be 21. If pure ` oxygen is used~or the combustion in the combustion chamber, S will be lO0.
, : : :
:: :
. 2~35~4 Detail~ of the automatic control in ac-cordance with the invention ~i.ll be ex~ained with reference to the illustrative embodiment of the process shown on the drawing~
The H2S-containing feed gas which is to be desulfurized is ~ed in line 1 to the combustion chamber 2 of a alaus process plantO Oxygen-containing gas is supplièd in line 3. '~he Claus process plant usu-ally comprises a plurallty of catalytic processi~g sta-ges, in which elementary sulfur is produced in accord- -.
ance with the (simplified) reaction equation 2 H2S ~
S2 = 3 S + 2 H20 from the gas mixture coming in line 4 from the combustion chamber 2. ~he sulfur i9 separated in a known manner, whlch is not shown hereO The drawing shows two catalytic ~rocessin~ stages 5 and 60 Part o~
the~elemen-tary sulfur Qay have been separated before the .`
catalytic stages by condensation from the gas mi~tuxe .. `:
coming from the combustion chamber 2. That ~as mixture flows -through the catalytlc processing stages 5 and 6 and then flows in line 7 to an analyzer 8, ~Jhich is incor- ` :
, porated in a branch line 7aO
he analyzer 8 detects the concentrations K and P of H2S and SO2 in the arrivi~ gas mixture, which :
is subseque~tly fed to the aftertreating means 9. In the aftertreating means the content o~ sulfur compounds in : ~: the~6as mixture is further decreased. The aftertreatment .
2 L3 3 ~
is not required in all cases and may be effected in known manner and in a plur~lity of parts or in a plula-lity of stages. The gas mixture is subsequently passed through afterburning means and is then discharged through a chimney 10 into the atmosphere.
il'he oxygen-containin~ ~as in line 3 is formed from a main stream supp~Lied in line 11 and of a supplemental stream supi)lied in line 12 and consisting of that ga;. ~he rates of said streams are cont~led by the flo~l control valves 1~ and 14. 'rO con-trol the rate of the maln stream in line 11, the rate of the feed gas in line 1 is measured b~ the flow meter ~
16 and -the rate signal is delivered via the signal line ~:
17 to a firs~ controller 18, w~lich acts on the flow oontrol valve 13 via the signal line 19. The same ra~e signal is delivered via à signal line 17a to a second controller 25 for adJusting the rate of the supplemental : stream of oxygen~containin; gas by means of the ~low c:ontrol valve 140 ~he flow meter 20 in line 11 indicates : ~ via the signal line 21 to the controller 18 the actual flow rate in line ll.
'l'he rate of the main stream of ~he oxygen-containing g~ fad to the combustion chamber 2 is ~::
co~trolled by means of the first controller 18. The secorld controller 25 serves also to e~ctly adjust the :~rate of supI)ly of oxygen to the combustion chamber 2 to - , :~ , ' ' '~:
: ~ "
2 ~ 5 ~7--the required value by a change of the rate of the supplementary s-tream comin from line 120 ~he control-ler 25 influences via the si~nal line 26 the flow control valve 14. In order -to determine the correction rate L by which the rate of the supplemental stream of oxygen~containing gas is to be chan~ed~ t~ correct- -ion rate ~ is calculated in the controller 25 i~ accord-ance with the formula ~ = D
S . .
The various parameters of said formula have been ex-plained hereinbefore. For the calculation of the cor-rection rate ~ the second controller 25 receives from the analyzer 8 via the signal li~e 8a the co~centration K of H2S and via the signal line 8~ the concen~ration -, . .~
P of S02 in the gas mixture which flo~ through -the anaIyzer. The -to~al rate ~i of oxygen-containing gas flowing in line 3 to the combustion chamber 2 is de-:~ ~te~mined by the meter 30 and the measured value is indi-cated via the signal line 31 to the controller 25, ~he flow meter 28 ln line 12 in~icates via the signal line 29~ to the oontroller 25 the rate at wbich oxygen-contain-ing g~s actually Elows through line 12 In a modification of the example illus-trated on the drawing the analy~er ~ :Eor measuring the ~ , concentrations of H2~ and S02 in the gas mixture may be ~arranged at different locations. ~he concentrations may ,, , ::, ~: : ' '' ~al3~
be analyzed upstream or do~vns-tream of any of ~he catalytic processin~ stages 5, 6 and upstr~am or downstream of a processin~ s~age which oelon~s to the aftertreatin~ means 9 or in such stage~ In -the embodi-ment of the process which is shown in the drawing the analyzer 8 is provided downstxeam of the last catalytic stage 6 of the Claus process I~lantO
.~xample In a processing s~stem as shown on the drawing, an H2S-containing feed ~a~ composed of H2S 7' mole ,'0 H2o 5.7 mole ,6 ~2 23.3 mole ~0 .
2H6 3r~0 mole ,~ -is fed at a rate of 8520~sm3/h to the combustion chamber 2 and is partly combusted therein with air supplied from~line 3 at a ra-te o~ 13793C:sm3/h. A main stream of th~ air is supplie:d at a rate of 12,510 sm3~h f~om : ~ . r : ~ : line 11 and a supplemental stream is supplied at a r~te of 1420 sm~/h from line 12. The Claus process plant con-tains arl A1203 catalyst in t~ro catal~tic sta~es 5 and 60 : Th~ analyzer 8 measures an H2S concentration I; of 0084 : mole percent: aDd an S0z concentratio~ P of 0.42 mole percentr. ~he desired value a:of the ratio K/~ is 2.00 ~: ~ '.' : ` ~
: ~ ; ~: :
., . . , . . . ..... , , - :: ; .: . . .
cj ,~
~ fter a ch~n~e of the concentratiion o~' H2S in the feed gas in J.ine 1 to 72 mole ~ercent, the ana-lyzer 8 will detect v.alues of E~ = 1049 mole percent and P - 0,32 mole percent. From a factor a = 2, S = 21 and a factor V = 0.412, which has been determined by a trial ::
operation, ~he controller 25 calculates the correction rate of air as ~ollows: ~
L = -Zl- (0.412 x 13,930 ~ 0.5 x 8520) = 404 sm3/h. ..
'~'' 3~ an adjustment of the flow control valve 14 the rate of air flowing in lines 12 and 3 is increased by that rate. .~s a result, an H2S concentration of 0~84 mole percent and an S02 concentration of 0~418 mole per-cent are rees~ablished in line 7 so that the desired ratio a = K~P = 2 is approxi~ated with ~ufficient accuracyD
The aftertreatment in 9 is pexformed by the Sulfreen ~rocess of Lurgi GmbH in Frankfurt on an A1203 catalyst by a re~ction of 2 H2S ~ S02 to 2 H2S +
3 SxO 600 p~m H2S and 300 ~rJm S02 are still found in the aft;ertreated gas. ~uel gas and air are added to~at gas, w~ich is then combusted and discharged into the atmos- .
phere O
, .
:: :
,~.', ; ' ,.';
~ ' . .
, . . . , ,, . " , ...
Claims (5)
1. A method of operating a plant for pro-ducing elementary sulfur, in which an H2S-containing feed gas is partly combusted with an oxygen-containing gas in a combustion chamber of a Claus process plant and a gas mixture that contains H2S and SO2 is thus produced, from which elementary sulfur is produced by a reaction of H2S with SO2 and is separated, wherein the reaction of the gas mixture coming from the combustion chamber is effected in one or more catalytic processing stages and optionally in aftertreating means, characterized in that the concentrations K and P of H2S and SO2 in the gas mixture are measured upstream or downstream of one of the catalytic processing stages or upstream or downstream of the aftertreating means or in such aftertreating means, the rate of feed gas flowing to the combustion chamber and the rate of supply of the oxygen-containing gas to the combustion chamber are measured, the results of said measurements are indicated to a controller and used to calculate the correction rate by which the rate of oxygen-, containing gas must be corrected to adjust the difference D = K - a x P to zero, wherein a is a factor that is specific to the process and lies between 0.1 and 10, and the rate of supply of oxygen-containing gas to the com-bustion chamber is changed by the correction rate.
2. A method according to claim 1, character-ized in that the stream of oxygen-containing gas supplied to the combustion chamber is formed from a main stream and a supplemental stream, the rates of the main stream and of the supplemental stream are con-trolled in dependence on the measurement of the rate of the feed gas, and the rate of the supplemental stream is in-creased or decreased by the calculated correction rate.
3. A process according to claim 2, character-ized in that the correction rate L (in sm3/h) is calculated in accordance with the formula wherein V = a factor that is specific to the process and lies between 0.01 and 2.0, D = the concentration difference K - a x P, measured in mole percent, E = rate of feed gas measured in sm3/h, S = percentage (in mole percent) of oxygen in the oxygen-containing gas, M = total rate (measured in sm3/h) of supply of the oxygen-containing gas to the combustion chamber.
4. A method according to claim 1, 2 or 3, characterized in that the concentrations K and P in the gas mixture are measured downstream of the last catalytic stage of a Claus process plant.
5. A method according to any of claims 1 to 3, characterized in that the concentrations K and P in the gas mixture are measured upstream or downstream of aftertreating means succeeding the Claus process plant or in said aftertreating means.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP4005378.4 | 1990-02-21 | ||
| DE19904005378 DE4005378A1 (en) | 1990-02-21 | 1990-02-21 | Process control in sulphur recovery by Claus process - by measuring hydrogen sulphide sulphide and sulphur di:oxide concn. and correcting combustion air supply |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2035554A1 true CA2035554A1 (en) | 1991-08-22 |
Family
ID=6400614
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2035554 Abandoned CA2035554A1 (en) | 1990-02-21 | 1991-02-01 | Method for the automatic control of the rate of supply of oxygen to a claus process plant |
Country Status (3)
| Country | Link |
|---|---|
| EP (1) | EP0444729A1 (en) |
| CA (1) | CA2035554A1 (en) |
| DE (1) | DE4005378A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7531135B2 (en) | 2004-07-13 | 2009-05-12 | D Haene Paul E | Process and system for controlling a process gas stream |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ATE229474T1 (en) | 1999-04-07 | 2002-12-15 | Boc Group Inc | TREATMENT OF GAS STREAMS CONTAINING HYDROGEN SULFIDE |
| EP3066046B2 (en) | 2013-11-08 | 2022-12-28 | Saudi Arabian Oil Company | Sulfur recovery unit and process |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3945904A (en) * | 1974-02-11 | 1976-03-23 | International Telephone & Telegraph Corporation | Process control system |
| FR2616241B1 (en) * | 1987-06-02 | 1990-12-07 | Elf Aquitaine | DEVICE FOR REGULATING THE OPERATION OF A CHEMICAL TREATMENT PLANT, FOR IMPROVING THE YIELD BY ATTENUATING THE VARIANCES OF THE ADJUSTMENT PARAMETERS |
-
1990
- 1990-02-21 DE DE19904005378 patent/DE4005378A1/en not_active Withdrawn
-
1991
- 1991-01-30 EP EP91200182A patent/EP0444729A1/en not_active Withdrawn
- 1991-02-01 CA CA 2035554 patent/CA2035554A1/en not_active Abandoned
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7531135B2 (en) | 2004-07-13 | 2009-05-12 | D Haene Paul E | Process and system for controlling a process gas stream |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0444729A1 (en) | 1991-09-04 |
| DE4005378A1 (en) | 1991-08-22 |
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