WO2004028963A1 - Process for the conversion of polysulfanes - Google Patents

Process for the conversion of polysulfanes Download PDF

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Publication number
WO2004028963A1
WO2004028963A1 PCT/EP2003/009432 EP0309432W WO2004028963A1 WO 2004028963 A1 WO2004028963 A1 WO 2004028963A1 EP 0309432 W EP0309432 W EP 0309432W WO 2004028963 A1 WO2004028963 A1 WO 2004028963A1
Authority
WO
WIPO (PCT)
Prior art keywords
polysulfanes
gas
process according
crude gas
vpm
Prior art date
Application number
PCT/EP2003/009432
Other languages
French (fr)
Inventor
Alexander Möller
Wolfgang BÖCK
Wolfgang Taugner
Harald Heinzel
Stephan Rautenberg
Original Assignee
Degussa Ag
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 Degussa Ag filed Critical Degussa Ag
Priority to US10/529,148 priority Critical patent/US7326393B2/en
Priority to JP2004538838A priority patent/JP4423199B2/en
Priority to AU2003255483A priority patent/AU2003255483A1/en
Priority to EP03798130A priority patent/EP1542925B1/en
Priority to BR0314663-4A priority patent/BR0314663A/en
Priority to DE60326604T priority patent/DE60326604D1/en
Publication of WO2004028963A1 publication Critical patent/WO2004028963A1/en
Priority to US11/976,717 priority patent/US7604788B2/en

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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
    • C01B17/16—Hydrogen sulfides
    • C01B17/167—Separation
    • 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
    • C01B17/16—Hydrogen sulfides
    • C01B17/168—Purification

Definitions

  • the invention relates to a process for the removal of polysulfanes from gas streams formed during H 2 S synthesis.
  • polysulfanes In H 2 S syntheses from hydrogen and sulfur, polysulfanes (HS n ) are generally found as by-products in the crude gas in an order of magnitude of > 400 vpm (volume per million) , and when the gas stream is compressed these tend to decompose in an uncontrolled manner into H 2 S and sulfur. This leads to undesirable sulfur deposits in the whole of the compression area, including the peripheral pipes and valves .
  • the high H 2 S concentration makes the shift of the equilibrium to the left-hand side seem probable and the decomposition of the polysulfanes into hydrogen sulfide and sulfur to be a non-preferred reaction.
  • the object of the invention is to provide a process for the practically complete removal of the polysulfanes, thus preventing sulfur deposits in the plant's pipes.
  • the invention provides a process for the removal of polysulfanes from crude gas formed during the production of hydrogen sulfide, characterized in that the crude gas, with a content of > 80 vol., preferably > 95 vol. H 2 S and > 100 to 2000 vpm, particularly > 400 to 1500 vpm, of polysulfanes (HS n with n: 2 to 8), is passed through an optionally multi-stage washer system, brought into contact with water and/or methanol, preferably with basic aqueous and/or methanol systems, and a pure gas is obtained in which the polysulfanes are present depleted by > 50 to > 99.5%, based on the starting value.
  • the quantities of polysulfanes can optionally also be more than 2000 vpm.
  • Jet washers are preferably used, which, like other washers, can be operated at a pressure of 1.05 to 10 bara, preferably at 1.05 to 2 bara.
  • Unpressurized operation is an alternative, however.
  • aqueous and/or methanolic 0.5 to 20 wt.%, preferably 0.5 to 10 wt.%, solutions of alkali hydroxides or oxides, especially OH/KHS or NaOH/NaHS solutions, are used as washing fluid.
  • the hydrogen sulfides are formed while passing the gas streams through the washing fluid.
  • the suitable temperature range is generally between 0 and 150°C, especially 10 and 60°C.
  • the polysulfanes are removed from the gas streams with a degree of depletion of > 50 to > 99.5%, preferably > 70 to > 99.5%, based on the starting content in the crude gas .
  • the sulfur formed during the conversion of the polysulfanes goes into solution, among other things as a result of the formation of the corresponding polysulfides .
  • Sulfur precipitated in solid form can optionally be discharged with the aid of suitable filtration devices.
  • the washing solution circulates and is discharged as a function of the polysulfide/sulfur load.
  • the washing fluid is topped up as a function of the rate of discharge and of quantities of solvent that may evaporate.
  • the H 2 S-containing gas is generally after-treated with the above-mentioned solutions in a washing column or a packed bed in counter-current (counter-current washer) . Entrained droplets are separated by means of a demister system. ⁇ Any quantities of sulfane remaining in the gas stream of purified H 2 S can also be broken down in a downstream adsorber bed (activated carbon, zeolite) and the sulfur formed can be separated off.
  • the polysulfane concentrations are dependent upon the reaction conditions in the HS reactor.
  • H 2 S crude gas was passed through an adsorption column packed with approx. 7 1 of etched Raschig rings at 20 Nm 3 /h.
  • the sulfur forming by decomposition of the polysulfanes was deposited on the surface of the packings. A degree of depletion of 25% was achieved. Service life of the adsorber bed 20 h.
  • H 2 S crude gas was passed through an adsorption column packed with approx. 7 1 of Si0 2 supports (particle size 3 - 5 mm) at 20 Nm 3 /h.
  • the sulfur forming by decomposition of the polysulfanes was deposited on the surface of the packings. A degree of depletion of 50% was achieved. Service life of the adsorber bed 48 h.
  • H 2 S crude gas was passed first through a jet washer system operated only with water and then through an adsorption column packed with approx. 12 1 of activated carbon (particle size 5 - 6 mm) at 200 Nm 3 /h for 60 h. Before entering the adsorption column, a degree of depletion of 75% and after the column a value of > 99% was measured.
  • H 2 S crude gas was passed first through a jet washer system supplied with methanol at 200 Nm 3 /h for 48 h. A degree of depletion of > 50% was achieved, based on the crude gas.
  • H 2 S crude gas was passed first through a washing column operated with a methanol/triethanolamine mixture (5% triethanola ine) for 24 h at 10 Nm 3 /h.
  • the sulfur forming as a result of decomposition of polysulfanes dissolved in the washing solution. A degree of depletion of 80% was • achieved.
  • Example 4 H 2 S crude gas was passed through a jet washer system supplied with a methanol/NaOH mixture (5% NaOH) for 400 h at 200 Nm 3 /h. A degree of depletion of 99% was achieved.
  • H 2 S crude gas was passed through a jet washer system supplied with a water/KOH mixture (12% KOH) for 200 h at 200 Nm /h. A degree of depletion of 99.5% was achieved.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Macromolecular Compounds Obtained By Forming Nitrogen-Containing Linkages In General (AREA)
  • Polymers With Sulfur, Phosphorus Or Metals In The Main Chain (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

The invention provides a process for the removal of polysulfanes from gas streams formed during H2S synthesis.

Description

Process for the Conversion of Polysulfanes
Field of the Invention
The invention relates to a process for the removal of polysulfanes from gas streams formed during H2S synthesis.
Background
In H2S syntheses from hydrogen and sulfur, polysulfanes (HSn) are generally found as by-products in the crude gas in an order of magnitude of > 400 vpm (volume per million) , and when the gas stream is compressed these tend to decompose in an uncontrolled manner into H2S and sulfur. This leads to undesirable sulfur deposits in the whole of the compression area, including the peripheral pipes and valves .
It is known that polysulfanes are thermodynamically unstable and have a tendency to decompose, particularly when heated (M. Schmidt, W. Siebert: "Sulfane" in Comprehensive Inorganic Chemistry, vol. 2, sect. 2.1, Perga on Press, Oxford 1973, 826-842).
Traces of alkali on the surface of glass vessels lead to the deposition of elemental sulfur.
However, these findings come from investigations with polysulfanes present in more or less pure form.
In principle, of course, they also apply to polysulfanes present in great dilution.
In this case, however, the influence of the concentration ratios has to be taken into account.
, Under the above circumstances, the polysulfanes are present in great dilution in hydrogen sulfide, which at the same time represents a decomposition product of the polysulfanes in a therrαodynamic equilibrium: χH2Sn =_=__ XH2S + ^11 SB
8
The high H2S concentration makes the shift of the equilibrium to the left-hand side seem probable and the decomposition of the polysulfanes into hydrogen sulfide and sulfur to be a non-preferred reaction.
The object of the invention is to provide a process for the practically complete removal of the polysulfanes, thus preventing sulfur deposits in the plant's pipes.
Summary of the Invention'
The invention provides a process for the removal of polysulfanes from crude gas formed during the production of hydrogen sulfide, characterized in that the crude gas, with a content of > 80 vol., preferably > 95 vol. H2S and > 100 to 2000 vpm, particularly > 400 to 1500 vpm, of polysulfanes (HSn with n: 2 to 8), is passed through an optionally multi-stage washer system, brought into contact with water and/or methanol, preferably with basic aqueous and/or methanol systems, and a pure gas is obtained in which the polysulfanes are present depleted by > 50 to > 99.5%, based on the starting value.
The quantities of polysulfanes can optionally also be more than 2000 vpm.
Detailed Description of the Invention
Jet washers are preferably used, which, like other washers, can be operated at a pressure of 1.05 to 10 bara, preferably at 1.05 to 2 bara.
Unpressurized operation is an alternative, however. In particular, aqueous and/or methanolic 0.5 to 20 wt.%, preferably 0.5 to 10 wt.%, solutions of alkali hydroxides or oxides, especially OH/KHS or NaOH/NaHS solutions, are used as washing fluid.
The hydrogen sulfides are formed while passing the gas streams through the washing fluid.
Appropriately concentrated solutions of other basic oxides or hydroxides, especially of alkaline earth hydroxides or oxides, preferably those of calcium, can also be used.
The polysulfanes are also removed from the gas streams by basic aqueous and/or methanolic 1 - 20%, preferably 1 to 10 wt.%, solutions of ammonia, organic amines, of the general formula (CnH2n+ι) XNHY with n=l, 2, 3; x = 2, 3; y=0, 1 or amino alcohols of the general formula (CnH2n+ιO) xNHy with n=l, 2, 3; x=2 , 3; y=0, 1.
The suitable temperature range is generally between 0 and 150°C, especially 10 and 60°C.
At gas velocities of the crude gas to be purified of generally between 0.1 and 25 m/s, especially 10 and 22 m/s, the polysulfanes are removed from the gas streams with a degree of depletion of > 50 to > 99.5%, preferably > 70 to > 99.5%, based on the starting content in the crude gas .
For a content of > 500 vpm in the crude gas, this corresponds to a depletion to < 10 vpm in the pure gas.
The sulfur formed during the conversion of the polysulfanes goes into solution, among other things as a result of the formation of the corresponding polysulfides .
Sulfur precipitated in solid form can optionally be discharged with the aid of suitable filtration devices.
The washing solution circulates and is discharged as a function of the polysulfide/sulfur load. The washing fluid is topped up as a function of the rate of discharge and of quantities of solvent that may evaporate. To remove any residual quantities of polysulfanes present after the jet washer (generally < 20% of, the starting quantity) , the H2S-containing gas is generally after-treated with the above-mentioned solutions in a washing column or a packed bed in counter-current (counter-current washer) . Entrained droplets are separated by means of a demister system. ■ Any quantities of sulfane remaining in the gas stream of purified H2S can also be broken down in a downstream adsorber bed (activated carbon, zeolite) and the sulfur formed can be separated off.
Analytical '
The analytical acquisition of the sulfane concentration in the crude .and pure gas takes place by means of an online UV measurement. Parallel to this, sulfur contents in the washing solution and sulfane and sulfur concentration in the H2S-containing gas stream are determined by wet- chemical means as required. ■
With the aid of the process according to the invention, it is possible to deplete the polysulfanes to such an extent that, in downstream processes, e.g. compressor stages, undesirable sulfur deposits are avoided..
Examples
Crude gases with a polysulfane content of > 400 to 2000 vpm are used.
The polysulfane concentrations are dependent upon the reaction conditions in the HS reactor.
Comparative Example 1
H2S crude gas was passed through an adsorption column packed with approx. 7 1 of etched Raschig rings at 20 Nm3/h. The sulfur forming by decomposition of the polysulfanes was deposited on the surface of the packings. A degree of depletion of 25% was achieved. Service life of the adsorber bed 20 h.
Comparative Example 2
H2S crude gas was passed through an adsorption column packed with approx. 7 1 of Si02 supports (particle size 3 - 5 mm) at 20 Nm3/h. The sulfur forming by decomposition of the polysulfanes was deposited on the surface of the packings. A degree of depletion of 50% was achieved. Service life of the adsorber bed 48 h.
Example 1
H2S crude gas was passed first through a jet washer system operated only with water and then through an adsorption column packed with approx. 12 1 of activated carbon (particle size 5 - 6 mm) at 200 Nm3/h for 60 h. Before entering the adsorption column, a degree of depletion of 75% and after the column a value of > 99% was measured.
Example 2
H2S crude gas was passed first through a jet washer system supplied with methanol at 200 Nm3/h for 48 h. A degree of depletion of > 50% was achieved, based on the crude gas.
Example 3
H2S crude gas was passed first through a washing column operated with a methanol/triethanolamine mixture (5% triethanola ine) for 24 h at 10 Nm3/h. The sulfur forming as a result of decomposition of polysulfanes dissolved in the washing solution. A degree of depletion of 80% was • achieved.
Example 4 H2S crude gas was passed through a jet washer system supplied with a methanol/NaOH mixture (5% NaOH) for 400 h at 200 Nm3/h. A degree of depletion of 99% was achieved.
The sulfur deposited after a running time of approx. 200 h was removed from the washer circulation with the aid of in-line filtration.
Example 5
H2S crude gas was passed through a jet washer system supplied with a water/KOH mixture (12% KOH) for 200 h at 200 Nm /h. A degree of depletion of 99.5% was achieved.

Claims

What is claimed is:
1. Process for the removal of polysulfanes from crude gas formed during the production of hydrogen sulfide, characterized in that the crude gas, with a content of > 80 vol.% H2S and > 100 to 2000 vpm, especially > 400 to 1500 vpm polysulfanes (H2Sn with n: 2 to 8) , is passed through a washer system, brought into contact there with water and/or methanol and a pure gas is obtained.
2. Process according to claim 1, characterized in that a 0.5 to 20 wt.% aqueous and/or methanolic solutions of an alkali or alkaline earth hydroxide or oxide is used as washing fluid.
3. Process according to claim 1, characterized in that 1 to 20 wt.% aqueous and/or methanolic solutions of organic amines of the general formula (CnH2n+ι)χNHγ with n=l ,2,3; x=2 , 3 ; y=0, 1 ; amino alcohols of the general formula (CnH2n+ιO)x Hγ with n=l,2,3; x=2 , 3 ; y=0,l or ammonia are used as washing fluid.
4. Process according to one or more of claims 1 to 3 , characterized in that a jet washer is used.
5. Process according to claims 1 to 4, characterized in that the pre-purified gas is after-treated in a counter-current washer with aqueous or methanolic solutions.
6. Process according to claims 1 to 4, characterized in that the gas depleted in polysulfanes is passed through an adsorber bed.
7. Process according to one or more of claims 1 to 6, characterized in that the polysulfanes contained in the crude gas are depleted in the pure gas at a rate of > 50 to > 99.5%, based on the crude gas. Process according to one or more of claims 1 to 7 , characterized in that the process is carried out at a temperature of 0 to 150°C.
PCT/EP2003/009432 2002-09-26 2003-08-26 Process for the conversion of polysulfanes WO2004028963A1 (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
US10/529,148 US7326393B2 (en) 2002-09-26 2003-08-26 Process for the conversion of polysulfanes
JP2004538838A JP4423199B2 (en) 2002-09-26 2003-08-26 Polysulfane conversion method
AU2003255483A AU2003255483A1 (en) 2002-09-26 2003-08-26 Process for the conversion of polysulfanes
EP03798130A EP1542925B1 (en) 2002-09-26 2003-08-26 Process for the conversion of polysulfanes
BR0314663-4A BR0314663A (en) 2002-09-26 2003-08-26 Process for polysulfan conversion
DE60326604T DE60326604D1 (en) 2002-09-26 2003-08-26 METHOD FOR CONVERTING POLYSULPHANES
US11/976,717 US7604788B2 (en) 2002-09-26 2007-10-26 Process for the conversion of polysulfanes

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10245164.8A DE10245164B4 (en) 2002-09-26 2002-09-26 Process for the conversion of polysulfanes
DE10245164.8 2002-09-26

Related Child Applications (2)

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US10529148 A-371-Of-International 2003-08-26
US11/976,717 Continuation-In-Part US7604788B2 (en) 2002-09-26 2007-10-26 Process for the conversion of polysulfanes

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US (1) US7326393B2 (en)
EP (1) EP1542925B1 (en)
JP (1) JP4423199B2 (en)
CN (1) CN1292980C (en)
AT (1) ATE425121T1 (en)
AU (1) AU2003255483A1 (en)
BR (1) BR0314663A (en)
DE (2) DE10245164B4 (en)
ES (1) ES2323060T3 (en)
RU (1) RU2323874C2 (en)
WO (1) WO2004028963A1 (en)

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WO2008087106A1 (en) * 2007-01-16 2008-07-24 Basf Se Method and device for the continuous production of hydrogen sulfide
JP2009507803A (en) * 2005-09-10 2009-02-26 エボニック デグサ ゲーエムベーハー Method for producing methyl mercaptan
CN101583563B (en) * 2007-01-16 2013-07-17 巴斯夫欧洲公司 Method and device for continuous production of hydrogen sulphide
EP2676925A1 (en) * 2012-06-22 2013-12-25 Evonik Industries AG Method and reactor for producing hydrogen sulphide
EP2676927A1 (en) * 2012-06-22 2013-12-25 Evonik Industries AG Method and reactor for producing hydrogen sulphide
EP2676926A1 (en) * 2012-06-22 2013-12-25 Evonik Industries AG Method and reactor for producing hydrogen sulphide
EP2676928A1 (en) * 2012-06-22 2013-12-25 Evonik Industries AG Method and reactor for producing hydrogen sulphide
US10773958B2 (en) 2014-03-21 2020-09-15 Chevron Phillips Chemical Company Lp Processes for removing polysulfanes and elemental sulfur from hydrogen sulfide

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US7604788B2 (en) * 2002-09-26 2009-10-20 Evonik Degussa Gmbh Process for the conversion of polysulfanes
CN101610976B (en) * 2007-01-16 2012-12-05 巴斯夫欧洲公司 Reactor and method for production of hydrogen sulphide
BE1018534A3 (en) 2007-07-11 2011-03-01 Basf Se PROCESS FOR THE SEPARATION WITH PURIFICATION OF ACRYLIC CRYSTALS, METHACRYLIC ACID, N-VINULPYRROLIDONE OR P-XYLENE FROM THEIR SUSPENSION IN A WASHING MACHINE.
JP4968207B2 (en) * 2008-07-31 2012-07-04 住友化学株式会社 A method for purifying hydrogen sulfide gas.
EP2382155B1 (en) 2008-12-23 2017-06-14 Basf Se Method for compressing gases containing hydrogen sulfide
EP2765127A1 (en) 2013-02-06 2014-08-13 Evonik Industries AG Process for the separation of acrolein from the process gas from the heterogeneously catalyzed oxidation of propene
CN111511677A (en) * 2017-12-25 2020-08-07 住友化学株式会社 Method for producing hydrogen sulfide and method for recovering sulfur

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JP2009507803A (en) * 2005-09-10 2009-02-26 エボニック デグサ ゲーエムベーハー Method for producing methyl mercaptan
WO2008087106A1 (en) * 2007-01-16 2008-07-24 Basf Se Method and device for the continuous production of hydrogen sulfide
US7833509B2 (en) 2007-01-16 2010-11-16 Basf Se Method and device for the continuous production of hydrogen sulfide
EP2460584A1 (en) * 2007-01-16 2012-06-06 Basf Se Apparatus for continuously preparing hydrogen sulfide
CN101583563B (en) * 2007-01-16 2013-07-17 巴斯夫欧洲公司 Method and device for continuous production of hydrogen sulphide
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US9421511B2 (en) 2012-06-22 2016-08-23 Evonik Degussa Gmbh Reactor and process for preparing hydrogen sulphide
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WO2013189715A1 (en) * 2012-06-22 2013-12-27 Evonik Industries Ag Reactor and process for preparing hydrogen sulphide
WO2013189718A1 (en) * 2012-06-22 2013-12-27 Evonik Industries Ag Reactor and process for preparing hydrogen sulphide
WO2013189712A1 (en) * 2012-06-22 2013-12-27 Evonik Industries Ag Reactor and process for preparing hydrogen sulphide
WO2013189719A1 (en) * 2012-06-22 2013-12-27 Evonik Industries Ag Reactor and process for preparing hydrogen sulphide
KR20150027226A (en) * 2012-06-22 2015-03-11 에보닉 인두스트리에스 아게 Reactor and process for preparing hydrogen sulphide
EP2676925A1 (en) * 2012-06-22 2013-12-25 Evonik Industries AG Method and reactor for producing hydrogen sulphide
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US9440208B2 (en) 2012-06-22 2016-09-13 Evonik Degussa Gmbh Reactor and process for preparing hydrogen sulphide
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US9630843B2 (en) 2012-06-22 2017-04-25 Evonik Degussa Gmbh Reactor and process for preparing hydrogen sulphide
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US10773958B2 (en) 2014-03-21 2020-09-15 Chevron Phillips Chemical Company Lp Processes for removing polysulfanes and elemental sulfur from hydrogen sulfide

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EP1542925B1 (en) 2009-03-11
EP1542925A1 (en) 2005-06-22
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RU2005112707A (en) 2006-01-27
CN1292980C (en) 2007-01-03
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ES2323060T3 (en) 2009-07-06
JP4423199B2 (en) 2010-03-03
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US7326393B2 (en) 2008-02-05
ATE425121T1 (en) 2009-03-15
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US20050265913A1 (en) 2005-12-01
CN1684905A (en) 2005-10-19

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