CA1313147C

CA1313147C - Desulphurisation

Info

Publication number: CA1313147C
Application number: CA000553656A
Authority: CA
Inventors: Patrick J. Denny
Original assignee: Imperial Chemical Industries Ltd
Current assignee: Imperial Chemical Industries Ltd
Priority date: 1986-12-24
Filing date: 1987-12-07
Publication date: 1993-01-26
Anticipated expiration: 2010-01-26
Also published as: NO875420L; US4861566A; EP0279116B1; JPS63175615A; NO167631B; EP0279116A3; DE3771062D1; NO167631C; GB8630846D0; NO875420D0; EP0279116A2

Abstract

Abstract Desulphurisation Fluid streams, particularly natural gas, are desulphurised by passage over a bed of a particulate absorbent containing zinc oxide at below 120°C. In order to increase the absorption capacity of the absorbent, the water and temperature of the fluid stream is controlled so that the stream both entering and leaving the absorbent bed has a degree of saturation of at least 30%, but does not contain a separate liquid aqueous phase.

Description

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Desulphurlsatlon This inventlon relates to desulphurisation and in - particular to the removal of sulphur compounds such as hydrogensulphide from fluid, ie gaseous or liquid, feedstock streams, particularly hydrocarbon streams such as natural gas. Such streams often contain substantial amounts of sulphur compounds, for example, where the hydrocarbon is gaseous, in an excess of 50 ppm by volume expressed as equivalent hydrogen sulphide.
Before use it is generally desirable to reduce the sulphur compounds content of the feedstock to a low level, for example to below 10 ppm by volume. One method of sulphur compound removal that is commonly employed is to contact the feedstock stream with a bed of particles of a suitable absorbent, such as zinc oxide. While a product stream of low sulphur content can be produced, such absorbents have only a limited capacity at low absorption temperatures and so, if large quantlties of sulphur compounds have to be removed, the beds need frequent replenishment.
We have found that the low absorption temperature capacity of certain zinc oxide-containing absorbents can be significantly improved if the feedstock contains a proportion of water.
It has been proposed in GB-A-1568703 to adjust the water vapour content of a synthesis gas stream, ie a gas stream containing hydrogen and carbon oxides, to 0.5 to 5% by volume prior to desulphurisation with a zinc oxide bed. In this reference the desulphurisation is preferably effected at temperatures above 200C. The object of incorporation of water vapour in the gas stream used in the process of that reference was to supress the formation of sulphur compounds such as carbonyl sulphide and carbon disulphide which are less readily removed than hydrogen sulphide from gas streams. Such compounds presumably result from the reactions:
H2S + C2 ----> H20 + COS
~2S + COS ----> H20 + CS2 ~313~7 These reactions are reverslble and so the formatlon of carbonyl sulphide and carbon disulphide is supressed by the incorporation of water in the gas stream. However the rate of such reactlons is believed to be very small at low temperatures and so carbonyl sulphide and carbon disulphide formation is unlikely to be a problem when effecting desulphurisation at low temperatures. The above reference has no appreciation that the presence of a controlled amount of water in the gas stream has the effect of increasing the absorption capacity of zinc oxide beds when operating at low absorption temperatures, and indeed suggests that the presence of water would be expected to be undesirable in view of the fact that the hydrogen sulphide absorption reaction produces water according to the equation H2S + ZnO ----> ZnS + H20 and so the presence of water might be expected to inhibit hydrogen sulphide absorption.
Accordingly the present invention provides a process for the removal of hydrogen sulphide from a fluid stream comprising passing the fluid stream, at a temperature below 120C, preferably below 80C, particularly below 50C, through a bed of a particulate zinc oxide-containing absorbent having a surface area above 50 m2.g 1, and controlling the water content and the temperature of the fluid stream such that the degree of saturation of the fluid stream with water is at least 30%, preferably above 50%, particularly above 80%, both as it enters and leaves the bed, but is such that there is no separate liquid aqueous phase in the stream entering and leaving the bed.
The particulate absorbent material preferably comprises at least 60%, especially at least 80%, by weight of zinc oxide, ca]culated on the constituents of the absorbent material non-volatile at 900C. As used in the process the zinc oxide may be, at least initially, wholly or partly hydrated or in the form of a salt of a weak acid, eg a carbonate, or basic carbonate.
The absorbent material is preferably in the form of porous agglomerates, as may be made, for example, by mixing a 1 3 1 3 1 ~ r~

finely divided æinc oxide composltion with a cement binder and a little water, insufficient to give a slurry, and then granulated or extruded. In order to aid access of the heated gas stream lnto the particles, the latter may be provlded ln the form of extruded pellets having a plurality of through passages. Typlcally the BET
surface area of the particles ls at least 50, preferably in the range 70 to 200, m2.g 1, and the pore volume of the particles is preferably at least 0.2 cm3.g 1.
Since the absorption efficiency and hence the life of a zinc oxide particulate bed depends on the rate of diffusion of the zinc sulphide formed by reaction of the zinc oxide with the sulphur compounds towards the interior of the particle, partlcularly at low absorption temperatures, it is preferable to employ zinc oxide particles having a high pore volume, above 0.2 cm3.g 1, and high surface area, above 50 m2 g 1. With zinc oxide particles having a lower pore volume and a surface area of the order of 25 to 30 m2.g 1 the effect of water enhancing the absorption capacity is not nearly so significant and so the bed life at low absorption temperatures is relatively low, necessitating the use of large bed volumes to avoid premature break-through of the sulphur compounds into the product stream. By using a bed of particles of pore volume above, for example, 0.25 cm3.g 1 and surface area above, for example, 70 m2.g 1, the bed volume can be markedly reduced, eg to about one third of that required with particles of low pore volume and surface area 25 to 30 m2.g 1. The particles employed thus preferably have a surface area above 70 m2.g 1 and a pore volume above 0.25 cm3.g 1.
Preferred particulate absorbent materials for the process have a hydrogen sulphide absorption capacity of at least 20%, especially at least 25%, of the theoretical, at a temperature of 25C, as determined in a standard test in which a mixture of hydrogen sulphide ~2000 ppm by volume), carbon dioxide (4% by volume), and methane (balance) is passed through a bed of the particles at atmospheric pressure and a space velocity of 700 h 1 using a bed of circular cross section having a length to :, .... : , . . : -~3131~1 ~ ~ 34150 diameter ratlo of 5.
A particularly suitable partlculate zinc oxide material is that sold by Imperial Chemical Industries plc as "Catalyst 75-1'`. These particles are granules typically havlng a surface area of the order of 80 m2~g 1 and a pore volume of about 0.5 cm3.g 1, and an adsorption capacity of about 27% of theoretlcal when measured by the above procedure.
Alternatively the particulate absorbent may comprise agglomerates of particles of an intimate mixture of oxides, hydroxides, carbonates and/or basic carbonates of copper, and zinc and/or at least one element such as aluminium as described in our copending Canadian patent application 535,574.

The inlet feedstock stream may be any gaseous or liquid that does not react with the absorbent. For example it ~ay be a hydrocarbon stream, such as natural gas or naphtha, and typically contains hydrocarbons containing an average of up to ten carbon atoms. Natural gas usually will contain, in addition to methane, one or more of ethane, propane, propene, butanes, and butenes.
The invention is also of utility with other feedstocks, for example air, carbon dioxide, halogenated hydrocarbons, eg chloro-and/or fluoro-carbons, phenols, or the product of fractionating a gas mixture produced by cracking or hydrocracking a normally liquid hydrocarbon feedstock, or the gaseous by-product of a zeolite-catalysed conversion of a feedstock such as methanol to gasoline. Preferably the fluid stream is substantially free from hydrogen and carbon monoxide.
The sulphur compounds initially present in the feedstock stream usually include hydrogen sulphide and/or carbonyl sulphide, and possibly carbon disulphide, methyl mercaptan, diethyl sulphide, and/or tetrahydrothiophene. The total initial concentration of hydrogen sulphide and/or of sulphur compounds readily hydrolysable thereto and expressed as sulphur equivalent hydrogen sulphide, is typically ln the range 10 ~o 1000 ppm by volume of the feedstock when the latter is in ~.,' ....

13131~7 the gaseous phase. The absorptlon can be conducted so that a substantial proportion, eg over 75~ by volume of the hydrogen sulphide, and of sulphur compounds readily hydrolysable thereto, can be removed. Typically the sulphur compounds content of the product is under 10, for example under 5, ppm by volume, expressed as above, but this is a matter of design, depending on the user's requirements.
In the process of the invention the temperature of the feedstock is typically in the range -10 to +120C. Where the feedstock contains insufficient water, water may be added by contacting the feedstock with liquid water, eg by passage through a saturator, prior to passage through the particulate absorbent - bed. Generally it is preferred to employ a feedstock having a temperature somewhat below the desired absorption temperature and to saturate it at that lower temperature, which is preferably about 3 to 10C below the desired absorption temperature, and to heat the resultant saturated gas stream to the desired absorption temperature, thereby reducing its degree of saturation to below 100%. Alternatively steam may be injected into the feedstock to add water and to increase the temperature.
The temperature of the fluid stream should be controlled so that the degree of saturation, ie relative humidity where the feedstock is gaseous, both of the fluid stream entering and leaving the absorbent bed, is above 30%, preferably above 50%, particularly above 80%, more particularly above 90%, and most preferably above 95%, but is such that no separate liquid aqueous phase is present in either stream. The reason for wishing to avoid the presence of a separate liquid aqueous phase is that pores of the high surface area absorbent materials tend to become blocked by the presence of liquid water hence restricting the access of the fluid stream to the absorbent material. Since, as described above, the absorption process produces water, it is important that not only is the water content of the fluid stream entering the bed of particulate absorbent such that no separate liquid aqueous phase is present, 13131~'~

6 B 34l50 but also that the lnlet water content is sufflclently low that a separate liquld aqueous phase wlll not result in the fluld stream leaving the absorbent bed. On the other hand the fluid entering, and leaving, the bed should have a high degree of saturatlon ln order that the beneflts of lncreased absorptlon capaclty of the bed are reallsed.
In some cases lt may be deslrable to provlde the bed wlth heatlng means so that the temperature thereof lncreases as the fluld stream passes through the bed. In thls way the lnlet and outlet degrees of saturation can be maintained closer to 100%. Alternatlvely lt may be deslrable to employ a plurality of absorbent beds ln serles and to provlde for partlal drying of the fluid stream, eg by means of a suitable adsorbent such as alumina or a molecular sieve, between beds ln order to avoid the ; lS deposltlon of a llquld aqueous phase.
The amount of water that the fluld contalns at any given degree of saturation will of course depend on the temperature and, in the case of gaseous feedstocks, also on the pressure. It is preferred that the fluid stream has a pressure from O.S to 120, particularly 1 to 100, bar abs.
The desulphurised fluid stream may be dried by means of a suitable absorbent, eg alumina or a molecular sieve, downstream of the particulate absorbent bed.
Wlthout wlshing to be limited it is thought that a possible explanation of the lncrease ln absorption capaclty of the bed resultlng from the presence of a controlled amount of water in the fluld stream is that the reaction mechanism for the absorption of hydrogen sulphlde by zinc oxide at low temperatures may involve the hydration of the surface layers of the zinc oxide, lndlcated in a simplistic form by the following equations ZnO + H20 ~ > Zn(OH)2 Zn(OH)2 + H2S ----> ZnS + 2H2 ln preference to the previously quoted equation ZnO + H2S ----> ZnS + H20 whlch is the prevalent mechanism at high temperatures and which 1313~ ~7 proceeds only 910wly at low temperat~lre~. The pre~ence of the hydroxyl groups may enhance the solld state dlffuslon reactions lnvolved ln the formation of zinc sulphide.
The invention is lllustrated by the followlng examples.
Example 1 Granules of slze approximately 3 to 5 mm of ICI
"Catalyst 75-1" were charged to a tube of internal diameter 2.54 cm to form a vertical bed of length 12 cm. The bed thus had a volume of about 60 ml. Natural gas, substantlally at atmospheric pressure and containing 1% by volume of hydrogen sulphide and 120 ppm by volume of water, was saturated by bubbling through water at 25C. The resultant gas thus contained about 2.5% v/v water and was then passed down through the bed malntained at about 30C
and atmospheric pressure at a rate of 700 ml/min, (le space velocity 700 hr 1).
The hydrogen sulphide content of the gas leaving the bed was monitored and when lt rose to 1-2 ppm by volume, indicating that hydrogen sulphide "break-through" had occured, the flow of gas was stopped and the absorbent discharged from the bed.
The absorbent was dlscharged in six equal parts A to F, so that the dlstribution of sulphur down the depth of the bed could be determined, and each part analysed, after drying at 105C, for its sulphur content. The results are shown in the following table.
The experiment was repeated but omitting the saturation step so that the gas stream contained only about 120 ppm by volume of water.

13~3~

_______ _______________________________~_________________ I I Sulphur content of discharged 1 I I absorbent (% w/w) I Bed portion 1-------- ----------------------I
1 1 2.5% H2O I 120ppm H20 l_________________________l______________l________________l I A (top) I 16.4 1 8.7 I B 1 15.2 1 9.2 I C 1 13.2 1 9.3 I D 1 11.0 1 8.7 I 5.9 1 5.1 I F (bottom) I 1.1 1 1.3 I A~erage 1 10.5 1 7.0 l_________________________l______________l________________l I Time to "break-through" I 6.25 hours 1 4 hours _________________________________________________________ It is seen that saturation of the gas stream at 25C
thus increased the capacity of the absorbent bed before "break-through" ocurred by about 50%.
In a comparative example the gas stream was passed through a dessicant prior to passage through the absorbent bed:
the results obtained were virtually identical with those quoted above for the gas containing 120ppm of water.
Example 2 The experiments of example 1 were repeated using gas streams containing 0.5% v/v hydrogen sulphide. The results are shown in the following table:

1313~7 __________________________________________________________ I I Sulphur content of discharged 1 I I absorbent (% w/w) I Bed portion l--------------------------------l 1 1 2.5~ H20 1 120ppm H20 l_________________________l_______________l________________l I A (top) I 19.7 1 8.4 I B 1 18.2 1 9.0 I C 1 15.6 1 8.7 10 I D 1 11.6 1 8.2 I E 1 5.8 1 4.5 I F (bottom) I 1.1 1 1.0 I Average 112.0 1 6.6 l_________________________l_______________l________________l 1. Time to "break-through" I 13.5 hours 1 6.5 hours __________________________________________________________ It is seen that in this case the capacity of the bed ; before "break-through" occurred was increased by about 82% by the presence of 2.5% water.
Example 3 The procedure of Example 1 was repeated using a gas stream containing 5%v/v hydrogen sulphide. In this example passage of the gas through the absorbent bed was continued for 25 hours, regardless of "break-through", in order to determine the 25 quantity of hydrogen sulphide that the bed could absorb. The results were as follows:

- 1313~ ~7 __________________________________________________________ I I Sulphur content of dlscharged I I absorbent (% w/w) I Bed portion 1---------------------------------1 1 1 2.5~ H20 1 120ppm H20 l________________________l_______________l_________________l I A ttop) 1 24.7 1 11.S
I B 1 23.4 1 12.4 I C 1 22.9 1 12.6 I D 1 22,9 1 13.1 I E 1 22.2 1 13.2 : I F ~bottom) I 23.3 1 14.0 I Average 1 23.2 1 12.8 __________________________________________________________ Again it is seen that the presence of 2.5% water in the gas stream resulted in an increase in the capacity of the absorbent bed of about 81%.
In a similar experiment wherein the water content of the gas stream was only 1% v/v, the increase in bed capacity was only about 30%.
In similar experiments performed with an absorbent bed temperature of 150C the increase in capacity of the absorbent bed given by the incorporation of about 2.5% v/v water was only about 8%.
Example 4 The procedure of Example 2 was repeated using differing absorption temperatures and differing degrees of saturation. In this case the sulphur content of that part of the bed having the greatest sulphur content is quoted in the following table:

``~-'` :
- ' : ' - ' 1313:~ ~7 I Absorption I Relative I Maximum I temperature I humidity at 1 sulphur I ~C) I absorption I content 1 I temperature (~ w/w) l________________l_________________l_____________l 1 5 10.3* 110.0 1 5 1100 117.5 125 10.4* 19.0 125 133 112.5 125 165 116.0 125 195 120.0 170 10.03* 110.1 170 110* 115.5 170 1100 123.0 1150 10.02* 117.5 1150 10.66* 120.0 1150 110.6* 126.5 Comparative It is seen that by having a high relative humidity the peak sulphur content obtained at low absorption temperatures could be increased to a level approaching that achievable at high absorption temperatures.
Example 5 The procedure of Example 2 was repeated using, instead of the "ICI Catalyst 75-1", agglomerates made by mixing precipitates obtained by precipitating copper, zinc and aluminium compounds as basic carbonates and/or hydroxides with calcium aluminate cement and a little water, granulating the resultant mixture, and drying and calcining the resultant granules for 4 hours at 350C to convert the basic carbonates and hydroxides to oxides. The calcined granules had a density of 1.1 g.cm 3, a BET
surface area of 105 m2.g 1, and an approximate Cu:Zn:Al atomic proportion of 51:26:23. In this example the "dry" gas contained 13 13 ~

about 20 ppm of water and the saturatlon and absorptlon temperature was 23C.
The results were as as set out in the following table:
_________________________________________________________ 1 I Sulphur content of discharged 1 I I absorbent (% w/w) I Bed portlon 1-------------------------------1 I I wet gas I dry gas l_________________________l______________l________________l 1 A (top) I 16.9 1 8.5 I B 1 16.2 1 8.5 I C 1 14.9 1 8.0 I D 1 14.6 1 8.8 I E 1 8.0 1 4.7 I F (bottom) I 1.3 1 0.6 I Average 1 12.0 1 6.4 l_________________________l______________l________________l I Time to "break-through" I 10.3 hours 1 5.9 hours _________________________________________________________ Example 6 Granules of size approximately 3 to 5 mm of ICI
"Catalyst 75-1" were charged to a tube of internal diameter 2.54 cm to form a vertical bed of length 18 cm. The bed thus had a volume of about 90 ml. Natural gas at 30 bar abs. and containing about 0.1% by volume of hydrogen sulphide, 2% by volume of hydrogen, and 180 ppm by volume of water, was saturated by bubbling through water at 23C. The resultant gas thus contained about 1100 ppm by volume of water and was then passed down through the bed maintained at about 23C and atmospheric pressure at a rate corresponding to a space velocity of 1000 hr 1 ~expressed at 1 bar abs. and 23C).
The hydrogen sulphide content of the gas leaving the bed was monitored and when it rose to about 1 ppm by volume, indicating that hydrogen sulphide "break-through" had occurred, the flow of gas was stopped and the absorbent discharged from the bed.

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The absorbent was discharged in six equal parts A to F, so that the distribution of sulphur down the depth of the bed could be determined, and each part analysed for its sulphur content. The results are shown in the following table.
The experiment was repeated but omitting the saturation step so that the gas stream was "dry" gas containing only about 180 ppm by volume of water.
_________________________________________________________ I I Sulphur content of discharged I
1 1 absorbent (~ w/w) I Bed portion 1-------------------------------l I I wet gas I dry gas l_________________________l______________l________________l I A (top) I16.0 1 13.1 I B 128.0 1 13.0 I C 127.2 1 10.6 I D 122.6 1 10.6 I E 118.2 1 8.6 I F (bottom) I 8.8 1 7.1 1 Average 120.1 1 10.5 I_________________________I______________I________________I
I Time to "break-through" I 156 hours 1 77 hours _________________________________________________________ It is believed that the low figure for the top of the bed results from liquid water entering the bed and blocking the pore of the top part of the bed.
Again it is seen that the use of "wet" gas greatly increased the absorption capacity of the bed.

PA/CG/MP
18 November 1987/L186A

Claims

1. A process for the removal of hydrogen sulphide from a gaseous stream comprising passing the gaseous stream at a temperature below 120°C through a bed of a particulate zinc oxide-containing absorbent having a surface area above 50 m2.g-1, characterised by controlling the water content and the temperature of the gaseous stream such that the degree of saturation of the gaseous stream with water is at least 30%, both as it enters and leaves the bed, but is such that there is no separate liquid aqueous phase in the stream entering and leaving the bed.

2. A process according to claim 1 wherein the gaseous stream is natural gas.

3. A process according to claim 1 wherein the gaseous stream is substantially free from hydrogen and carbon monoxide.

4. A process according to claim 1 wherein the water is added by contacting the gas with liquid water so as to saturate the gas and then increasing the temperature of the gas by 3°-10°C prior to contact of the gas with the absorbent.

5. A process according to claim 1 wherein the absorption temperature is below 50°C.

6. A process according to claim 1 wherein the degree of saturation of the gaseous stream entering and leaving the bed is above 80%.

7. A process according to claim 1 wherein the absorbent comprises porous agglomerates having a pore volume of at least 0.25 cm3.g-1 and a surface area above 70 m2.g-1.