CA1101639A - Method for increasing the hydrogen sulphide concentration in an acid gas - Google Patents

Method for increasing the hydrogen sulphide concentration in an acid gas

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Publication number
CA1101639A
CA1101639A CA293,724A CA293724A CA1101639A CA 1101639 A CA1101639 A CA 1101639A CA 293724 A CA293724 A CA 293724A CA 1101639 A CA1101639 A CA 1101639A
Authority
CA
Canada
Prior art keywords
gas
absorber
value
absorbent
magnitude
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
CA293,724A
Other languages
French (fr)
Inventor
Jan Verloop
Johannes W.T.M. Braam
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Canada Ltd
Original Assignee
Shell Canada Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shell Canada Ltd filed Critical Shell Canada Ltd
Application granted granted Critical
Publication of CA1101639A publication Critical patent/CA1101639A/en
Expired legal-status Critical Current

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Classifications

    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/02Preparation of sulfur; Purification
    • C01B17/04Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404Preparation 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
    • C01B17/0408Pretreatment of the hydrogen sulfide containing gases
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1412Controlling the absorption process
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425Regeneration of liquid absorbents
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456Removing acid components
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456Removing acid components
    • B01D53/1468Removing hydrogen sulfide
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/16Hydrogen sulfides
    • C01B17/167Separation
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/151Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Abstract

A B S T R A C T

A method for increasing the hydrogen sulphide concen-tration in an acid gas, the acid gas being supplied to a selective absorber, in which the gas is contacted with an absorbent, which is subsequently supplied to a regenerator, in which gas is liberated from the absorbent, characterized in that a value is determined for the magnitude of the gas stream passing to the absorber; that, if this value is smaller than a predetermined value, a proportion of the liberated gas is passed to a second selective absorber, in which it is contacted with a proportion of the regenerated absorbent originating from the regenerator, which, likewise loaded, is subsequently supplied to the regenerator and that if this value again exceeds a second predetermined value the gas stream to the second absorber is stopped.

Description

The invention relates to a method for increasing the hydrogen sulphide concentration in an acid gas, the acid gas being supplied to a selective absorber wherein the gas is contacted with an absorbent, which is subsequently supplied to a regenerator in which the gas is liberated from the absorbent.
By acid gas is meant: gas containing H2S and C02, such as natural gas, refinery gas and gas formed during partial combustion of sulphur-containing hydrocarbons and/or coal.
~ he absorbent used is very suitably an aqueous solution of a basic compound, such as alkalimetal carbonates and phosphates. Preference is given to liquid absorbents consisting of an aqueous solution of an amine. The amines may be primary, secondary or tertiary amines or mixtures thereof. Ethanol amine may be mentioned as an example; preference is given to polyalkanol amines, in particular di-isopropanol amine and methyl diethanol amine.
If desired the aqueous solution of an amine may also contain non-basic compounds capable of physically absorbing H2S and C02. Examples of this type of compounds are N-methyl-pyrrolidone, methanol and cyclotetramethylene sulfones, in particular sulfolane.
The acid constituents of the acid gas are absorbed into the absorbent at 10W temperature; the solvents in turn release the said acid constituents readily at high temperature.

:` ~

~k ~ 4 To that end the loaded absorbent is supplied to a regenerator, in which ~he separation is effected in SUC~I a manner that a mixture of predominantly hydrogen sulphide and carbon dioxide is released at the top and the sub-stantially clean solvent at the bottom.
The resultant gas mixture is preferably supplied to a unit in which the hydrogen sulphide is converted into elemental sulphur, such as according to the Claus process. In this unit, a proportion of the H2S is oxidized to S02, which in reaction with the remaining H2S, possibly under the effect of a suitable catalyst, forms sulphur and water. This conversion of H2S into elemental sulphur proceeds more readily when the H2S concentration in the acid gas is above a certain minimum value. Thus, special measures become necessary if the H2S concentration is lower than 15%. An H2S con-centration of less than 2% renders the use of the Claus process, even with special measures, such as direct oxidation or fuel gas injection, no longer ~
attractive. t The object of the invention is to provide a method for automatically increasing the concentration of hydrogen sulphide in an acid gas which method is reliable, simple to perform, relatively less expensive and moreover flexible.According to the present invention there is provided a method for increasing the hydrogen sulphide concentration in an acid gas, the acid gas being supplied to a selective absorber, in which the gas is contacted with an absorbent, which is subsequently supplied to a regenerator, in which gas is liberated from the absorbent, characterized in that a value is determined for tne magnitude of the gas stream passing to the absorber; that, if this value is smaller than a predetermined value, a proportion of the liberated gas is passed to a second absorber which preferentially absorbs hydrogen sulphide, wherein the liberated gas is contacted with a proportion of the regenerated absorbent originating from the regenerator, which, likewise loaded, is sub-sequently supplied to the regenerator and that if this value again exceeds a second predetermined value the gas stream to the second absorber is stopped.

3~

The magnitude of the gas stream determines, among other things, the degree in which the absorbent also absorbs carbon dioxide, in such a way that if there is a small gas stream, much more C02 is absorbed than if this stream has a high value. The gas liberated from the absorbent after regeneration contains not only hydrogen sulphide but also carbon dioxide. Now if, for example, the hydrogen sulphide represents only 2% of the total quantity of gas, then it is not desired to pass this gas stream to the Claus process.
According to the invention a proportion of the liberated gas stream is passed to a second absorber, in which the conditions ;~
are so selected that preferably H2S is absorbed in the absorbent, or, in other words, that H2S is selectively removed from the gas stream. The resultant loaded absorbent is also passed from the second absorber to the regenerator, where the gas is liberated from the absorbent, as is the gas originating from the loaded absorbent of the first absorber. It will now be clear tha~ the combined gas stream originating ' ' ~

L6;39 originating from the regenerator has a higher hydrogen sulphide content than the gas leaving the regenerator before the second absorber was actuated. A
new equilibrium adjusts itself at a desired HzS concentration. If, subse-quently, the gas stream to the first absorber begins to increase again, at a certain moment the situation will be reached that the measured value exceeds a second predetermined value whereupon the gas stream to the second absorber is stopped. Preferably this second predetermined value is selected larger than the first predetermined value in order to be sure that this automatical-ly proceeding process continues to be controlled in a stable manner.
At the moment that it is established that the magni-tude of the in-coming gas stream has become too small, the H2S concentration of the dis-charged gas is still sufficient, to the extent of course that the quantity of H2S in the supplied gas remains reasonably constant; the effect of the re-duced supply will only become felt at the outlet of the plant after some time. Hence the control of the gas stream to the second absorber must only be initiated some time after the reduced supply has been observed. In order to have the second absorber in operation at the moment when tbe gas begins to flow to this absorberj the absorbent circulation is generally started imme-diately the magnitude of the quantity of the gas flowing to the first ab-sorber has fallen below a certain desired valuej a corresponding signal is subsequently passed via a delay device to open the line through which the gas is passed to the second absorber. ~;
If the hydrogen sulphide concentration in the supply to the first absorber is not substantially constant, it is preferred when comparing the value of the quantity with the predetermined value also to take into con-sideration the concentration of hydrogen sulphide in the liberated gas. In this way it is possible to keep the quality, i.e. the H2S concentration of the liberated gas, within certain limits.
The invention will now be further elucidated with reference to the drawing, in which:

63~

Figure 1 shows diagrammatically the plant in which the method according to the present invention can be carried out;
Figure 2 shows the magnitude of the various process streams as a function of the magnitude of the gas stream to the plant in Figure 1.
In Figure 1, reference numeral 1 designates an absorber in which at 2 an acid~gas is supplied and at 3 an absorbent which absorbent, loaded with acid constituents from the gas leaves the absorber at the bottom at 4, assisted by a pump 5. At the top of the absorber at 6 the remaining gas is discharged, through a line 7, to for example a combustion furnace (not shown).
The liquid level in the absorption column 1 is controlled by means of a level controller 8, and a control valve 9, incorporated in the delivery line 10 of the pump 5. The loaded absorben-t is supplied -through the line 10 into the top of a regenerator 11, in which the acid gas consti-tuents are again separat-ed from the absorbent in such a way that clean absorbent leaves the regener-ator through the bottom at 12, and the acid gas constituents, largely compris- `
ing hydrogen sulphide and carbon dioxide, leave the regenerator at the top at 13. This acid gas mixture is passed through the line 14 to for example a Claus process (not shown) in which the hydrogen sulphide is converted into elemental sulphur. The supply line 15 for the acid gas to the absorber 1 is provided with a flow meter and transmitter 16, which determines the magnitude of the gas stream and generates a corresponding signal which is then passed to a computing device 17. To this computing device is also supplied a signal b originating from a meter and transmitter 18 which is incorporated in the line 14 and determines the hydrogen sulphide concentration in the gas flowing through the line. The output signal c from the computing device 17 depends on the signals a and b as follows:
c = -fa ~ kb in which f and k represent constants.
This signal c is passed to a solenoid valve 19, which allows the signal to pass to a flow controller 20 as soon as the said valve is opened under the ef~ect o~ a signal which is generated at the output of the switch 21 if c is larger than a first predetermined value. If c subsequently falls below a second predetermined value, the switch 22 will produce a signal with which the valve is closed. The signal at the output o~ switch 21 passes a delay device 23 on its way to the valve 19, as a result of which some time passes between the arrival o~ the signal at the input of the said element 23 and the arrival of the slgnal at its output and consequently at the valve 19.
The output of the s~itch 21 is ~urther connected with a solenoid valve 24, which is opened by the signal originating from switch 21, while the said sig-nal also serves to start the pump 25 through the switch 26. As soon as the valve 19 opens the signal c is allowed through to the ~low controller 20, which operates a valve 27 in a branch 28 o~ the gas line 14 in such a way that it opens with the result that the gas is allowed to ~low at 29 into a second absorber 30. The ~low meter and transmitter 31' in the gas line 28 `~
.
measures the magnitude of the gas stream concerned and passes a corresponding signal g to a computing device 31 in which by means of a predetermined set value h the equation:
p = qg + h is generated, in which q represents a constant value. The signal p is passed through the already open valve 24 to a ~low controller 32, which operates a valve 33 in the line 34, which debouches a-t 35 in the top o~ the absorber 30.
The clean absorbent leaving the regenerator 11 at 12 is drawn in pump 36 through the line 37 and delivered into the line 38 which branches into the above-mentioned line 34 and a line 39, which latter debouches in the first absorber 1 at 3. A ~low controller 40 with a corresponding control valve 41 ensures that the total stream o~ absorbent remains constant. The quantity o~ absorbent flowing to the second absorber 30 is controlled by the controller 32 with the corresponding control valve 33.
The loaded absorbent leaves the absorber 30 through the bottom at 42 and is pumped by pump 25 through the delivery line 43 into the line 10, ~0~639 through which the loaded absorbent is passed to the regenerator 11. The liquid level in the absorber 30 is held at a certain minimum value by means of a level controller 44 and a corresponding control valve 45 The system described above works as follows: if the magnitude of the gas stream passing to the firs-t absorber 1 decreases, the signal a will decrease and consequently the signal c will increase until it exceeds a cer-tain predetermined value, after which the valve 24 is opened by means of the switch 21. The signal p is now passed to the controller 32 as a result of which valve 33 opens and the inflow of solvent into the absorber 30 at 35 is made possible. After some time, as a result of the delay element 23, the valve 19 opens. A proportion of the gas stream which i5 transported through the line 14 to a subsequent process, such as a Claus process, will now be passed through the line 28 to the absorber 30. The latter absorber will be so chosen that substantially all the hydrogen sulphide is absorbed from the gas in the absorbent, while most of the carbon dioxide is discharged at 46 through the line 47 to the discharge line 7, which leads for example to a combustion furnace (not shown). The loaded absorbent is passed to the regen-erator 11, where the gas is separated from the solvent, with the result that the concentration of hydrogen sulphide in the gas stream leaving the regener-ator at 13 has increased, in which way a new equilibrium adjusts itself atwhich the H2S concentration is at a higher value than if no gas were passed to the second absorber 30. It is ensured by means of the controller 18 that the quality of the gas in the line 14, i.e. the H2S content of -this gas, re-mains constant, at least within certain limits.
Instead of a relatively expensive quality controller it is possible to use a flow controller at this location if the quality of the feed gas up-stream of the plant, i.e. the quality of the gas introduced through line 15 into the first absorber 1 at 2, is constant or substantially constant.
If the feed stream increases again the signal c becomes smaller.
As soon as a certain minimum value is exceeded the switch 22 is actuated.

3~

The output of this switch 22 is directly connected with the valve 19, which is now closed with the result that the valve 27 also closes and the gas stream through the line 28 is therefore stopped. This output is further con-nected via a delay device 48 with the valve 24 which, some time after the gas stream stops, is thus closed at -the same time as the pump 25. The valve 21l is fitted with a needle valve 49 which ensures that the set signal p can de-cay only slowly so that the valve 33 in the solvent line 34 also closes slowly.
Figure 2 represents schematically the magnitude in m3 of the var-ious streams of the plant from Figure 1, as a function o-f the percentage of the design capacity of the installation for treating a gas i.e. the gas sup-plied through the line 15 into this plant. Curve A relates to -the magnitude of the gas stream theoretically to be recycled, i.e. the stream in line 28;
curve B relates to the magnitude of the theoretically required absorbent stream which would be introduced into the absorber 1 at 3; curve C relates to the magnitude of the theoretically required absorbent stream which would be introduced into the absorber 30 at 35, and curve D relates -to the algebraic sum of these two absorbent streams, in other words the stream in line 38. As has been mentioned above, these curves represent the theoretically required quantities. These theoretically calculated quantities are approximated by means of the control system described with reference to Figure l; the magni-tude of the actual streams will therefore depend linearly on the stated per-centage of the design capacity of the plant. Lines A', A", A"', B', C' and D' therefore each represent the actual relationship which may exist between the said quantities. In the figure the situation is represented in which the valve 27 in the line 28 is opened as soon as the quantity of gas flowing into the plant through the line 15 falls to only 80% of the design capacity. ~he valve 27 then opens so far that the quantity H of gas is passed to the ab-sorber 30, in which the quantity K of absorbent is already circulating. It is assumed in this respect that the quality, i.e. the H2S content, of the gas . ~

in line 14 is at a desired level, since the quality of the gas in the line 14 is a measure of b and therefore of c according to the equation:
c = -fa + kb. Figure 2 sbows this relationship for three values of b, a desired value; line A'; a lowest admissible value, line A " ; and a maximum admissible value of B: line A " '. The figure further shows tha-t the valve 27 is closed, such that the gas stream to the second absorber stops, as soon as the gas supply to the line 15 has reached such a value that the signal c becomes smaller than the value c2 as a result of which (see Figure 1) the solenoid valve 19 is closed and a~ter some delay the solenoid valve 24, as a result of which -the absorbent circulation in the second absorber will also gradually stop.
The theoretically required quantity of absorbent can be determined by means of the curved B and C for the first and second absorber respectively, the total required quantity is the algebraic sum of the above-mentioned quan-tities and can be determined by means of curve D. Preferably, in practice the total quantity of absorbent in the plant is held continuously constant in such a manner that the substantially horizontal line D' represents this con-stant quantity of solvent. ~ow if a quantity of solvent K begins to circu-late in the second absorber, this will be at the expense of the quan-tity which initially circulated in the first absorber, so that this quantity falls to a valùe L, which is nevertheless amply sufficient.
It will be quite clear that the invention is not limited to the em-bodiment described above, which is given only by way of example. In partic-ular it is perfectly possible, without departing fro-m the conception of the invention, to allow the control of the quantity of gas passed to the second absorber to depend on the magnitude of the gas stream to the first absorber:
signal a, and on the quality of the discharged gas: signal b, according to the equa-tion:
m.a c n.b ~

`: :

~ 3L63~
, .

in which m and n represent constants.
As has been remarked above, the meter 18 for the quality of the discharged gas need not necessarily be a quality me-ter capable of measuring the H2S concentration in the gas, but, provided that the quality o~ the gas supplied to the first absorber is substantially constant, it may also be a flow meter. ~his meter, however, is not at all necessary for achieving the primary object of the invention, since the measurement of the quantity of supplied gas, certainly if its quality is substantially constant, provides already sufficient information with respect to the probable quality of the gas to be discharged.

..;
,'

Claims (8)

THE EMBODIMENTS OF THE INVENTION IN WHICH AN EXCLUSIVE
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A method for increasing the hydrogen sulphide concentration in an acid gas, the acid gas being supplied to a selective absorber, in which the gas is contacted with an absorbent, which is subsequently supplied to a regenerator, in which gas is liberated from the absorbent, characterized in that a value is determined for the magnitude of the gas stream passing to the absorber; that, if this value is smaller than a predetermined value, a proportion of the liberated gas is passed to a second absorber which preferentially absorbs hydrogen sulphide, wherein the liberated gas is contacted with a proportion of the regenerated absorbent originating from the regenerator, which, likewise loaded, is subsequently supplied to the regenerator and that if this value again exceeds a second predetermined value the gas stream to the second absorber is stopped.
2. A method as claimed in claim 1, characterized in that when actuating the second absorber the absorbent circulation is started first and that after some time the supply of the gas to the second absorber is made possible.
3. A method as claimed in claim 1 or 2, characterized in that the quantity of the gas flowing to the second absorber is measured and that the magnitude of the absorbent circulation in the second absorber is controlled in dependence on this quantity.
4. A method as claimed in claim 1, characterized in that when shutting down the second absorber out of operation the gas stream is shut off first and after some time the absorbent circulation.
5. A method as claimed in claim 1 characterized in that when comparing the value of the magnitude of the gas stream passing to the absorber with the predetermined value the hydrogen sulphide concentration in the liberated gas is also taken into consideration.
6. A method as claimed in claim 1, characterized in that when comparing the value of the magnitude of the gas stream passing to the absorber with the predetermined value the magnitude of the stream of liberated gas is also taken into consideration.
7. A method as claimed in claim 5 or 6, characterized in that a value c is calculated from the value of the magnitude a of the gas stream passing to the absorber and the value b of the hydrogen sulphide concentration in the liberated gas or the magnitude of the stream of liberated gas according to:
c = -fa + kb, in which f and k represent constants and that the value of c calculated in this way is compared with a predetermined value.
8. A method as claimed in claim 5 or 6, characterized in that a value c is calculated from the value of the magnitude a of the gas stream passing to the absorber and the value b of the hydrogen sulphide concentration in the liberated gas or the magnitude of the stream of liberated gas according to: c = , in which m and n represent constants and that the value of c calculated in this way is compared with a predetermined value.
CA293,724A 1977-02-04 1977-12-22 Method for increasing the hydrogen sulphide concentration in an acid gas Expired CA1101639A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL7701175A NL7701175A (en) 1977-02-04 1977-02-04 METHOD FOR INCREASING THE CONCENTRATION OF HYDROGEN HYDROGEN IN AN ACID GAS
NL7701175 1977-02-04

Publications (1)

Publication Number Publication Date
CA1101639A true CA1101639A (en) 1981-05-26

Family

ID=19827920

Family Applications (1)

Application Number Title Priority Date Filing Date
CA293,724A Expired CA1101639A (en) 1977-02-04 1977-12-22 Method for increasing the hydrogen sulphide concentration in an acid gas

Country Status (13)

Country Link
US (1) US4210627A (en)
JP (1) JPS5397995A (en)
AU (1) AU516293B2 (en)
BE (1) BE863281A (en)
BR (1) BR7800664A (en)
CA (1) CA1101639A (en)
DE (1) DE2804452A1 (en)
FR (1) FR2379311A1 (en)
GB (1) GB1563671A (en)
NL (1) NL7701175A (en)
SU (1) SU1069619A3 (en)
TR (1) TR20214A (en)
ZA (1) ZA78645B (en)

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DE2854060A1 (en) * 1978-12-14 1980-07-03 Linde Ag METHOD FOR PROVIDING A REPLACEMENT GAS FOR A CHEMICAL REACTION AND FOR SEPARATING A GAS SHAPED REACTION PRODUCT
US4397661A (en) * 1980-06-27 1983-08-09 Monsanto Company Gas permeation apparatus having permeate rate controlled valving
US4289738A (en) * 1980-07-22 1981-09-15 The Dow Chemical Company Process for removing H2 S from sour gases with generation of a Claus feed gas
GB2100471B (en) * 1981-05-28 1985-03-06 British Gas Corp Automatic coi removal system and operation thereof
US5266274A (en) * 1992-10-13 1993-11-30 Tpa, Inc. Oxygen control system for a sulfur recovery unit
US5556606A (en) * 1994-10-07 1996-09-17 Khanmamedov; Tofik K. Method and apparatus for controlling the hydrogen sulfide concentration in the acid gas feedstock of a sulfur recovery unit
WO1996014135A1 (en) * 1994-11-03 1996-05-17 Khanmamedov Tofik K Method and apparatus for removal of contaminates from refinery gas
US6506349B1 (en) 1994-11-03 2003-01-14 Tofik K. Khanmamedov Process for removal of contaminants from a gas stream
US6372126B1 (en) * 1999-07-19 2002-04-16 Gary R. Reeves Chlorinator for aerobic waste treatment systems
CA2605520C (en) * 2005-04-20 2010-11-02 Fluor Technologies Corporation Configurations and methods for claus plant operation with variable sulfur content
US8226893B2 (en) * 2008-06-24 2012-07-24 Mclauchlan Robert A Automated sulfur recovery loop
US20100219061A1 (en) * 2009-03-02 2010-09-02 Saudi Arabian Oil Company Enhancement of acid gas enrichment process
JP5693295B2 (en) * 2011-02-28 2015-04-01 三菱重工業株式会社 CO2 recovery device and operation control method of CO2 recovery device
JP5494754B2 (en) * 2012-07-31 2014-05-21 住友金属鉱山株式会社 Hydrogen sulfide gas production plant system and method of recovering and using hydrogen sulfide gas
JP5708849B2 (en) * 2014-02-27 2015-04-30 住友金属鉱山株式会社 Hydrogen sulfide gas production plant system and method of recovering and using hydrogen sulfide gas

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US3333398A (en) * 1967-08-01 Absorption flow control
US2614904A (en) * 1946-12-04 1952-10-21 Koppers Co Inc Gas separation
BE626408A (en) * 1961-12-27
JPS496297B1 (en) * 1969-03-15 1974-02-13
IT1048269B (en) * 1973-03-01 1980-11-20 Shell Int Research PROCESS TO REDUCE THE TOTAL CONTENT OF EXHAUST GAS SULFUR OF THE CLAUS PROCESS

Also Published As

Publication number Publication date
BE863281A (en) 1978-07-25
AU3294278A (en) 1979-08-09
DE2804452C2 (en) 1987-01-22
DE2804452A1 (en) 1978-08-10
AU516293B2 (en) 1981-05-28
SU1069619A3 (en) 1984-01-23
NL7701175A (en) 1978-08-08
BR7800664A (en) 1978-09-26
ZA78645B (en) 1978-12-27
TR20214A (en) 1980-10-17
FR2379311B1 (en) 1982-04-23
JPS5397995A (en) 1978-08-26
US4210627A (en) 1980-07-01
GB1563671A (en) 1980-03-26
FR2379311A1 (en) 1978-09-01

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