WO2004105922A1

WO2004105922A1 - A process for the removal of so2, hcn and h2s and optionally cos, cs2 and nh3 from a gas stream

Info

Publication number: WO2004105922A1
Application number: PCT/EP2004/050955
Authority: WO
Inventors: Petrus Franciscus Antonius Van Grinsven; Wiebe Sjoerd Kijlstra; Inge Roos; Cornelis Jacobus Smit
Original assignee: Shell Internationale Research Maatschappij B.V.
Priority date: 2003-05-29
Filing date: 2004-05-28
Publication date: 2004-12-09
Also published as: DE602004014923D1; EP1628744B1; US7655205B2; US20060272502A1; ATE400350T1; CN100376313C; ES2308194T3; CN1798600A; EP1628744A1

Abstract

The invention relates to a process for the removal of S02, HCN and H2S and optionally one or more compounds from the group of COS, CS2 and NH3 from a first gas stream, which process comprises the steps of: (a) removing S02 from the first gas stream by contacting the first gas stream in a hydrogenation zone with a hydrogenation catalyst in the presence of hydrogen to obtain a second gas stream; (b) removing HCN and optionally COS and/or CS2 from the second gas stream obtained in step (a) by contacting the second gas stream in a hydrolysis zone with a hydrolysis catalyst in the presence of water to obtain a third gas stream; (c) removing NH3 from the third gas stream by contacting the third gas stream in a NH3-removal zone with an aqueous acidic washing liquid to obtain an ammonium-comprising aqueous stream and a fourth gas stream; (d) removing H2S from the fourth gas stream by contacting the fourth gas stream in a H2S-removal zone with an aqueous alkaline washing liquid to obtain a H2S-depleted gas stream and a hydrogensulphide-comprising aqueous stream; (e) contacting the hydrogensulphide-comprising aqueous stream obtained in step (d) with sulphide-oxidizing bacteria in the presence of oxygen in an oxidation reactor to obtain a sulphur slurry and a regenerated aqueous alkaline washing liquid; (f) separating at least part of the sulphur slurry obtained in step (e) from the regenerated aqueous alkaline washing liquid and; (g) recycling regenerated aqueous alkaline washing liquid obtained in step (e) to the H2S-removal zone in step (d).

Description

A PROCESS FOR THE REMOVAL OF S0₂, HCN AND H₂S AND OPTIONALLY COS, CS AND NH3 FROM A GAS STREAM

The invention relates to a process for removing S0₂, HCN and H₂S and optionally COS, CS₂ and NH3 from a gas stream.

Gas streams from industrial chemical processes may contain a variety of sulphur compounds such as H S, S0 , CS₂ and COS. The removal of these sulphur compounds is of considerable importance, because the toxicity and smell of sulphur compounds renders their presence highly undesirable. In addition, other compounds whose presence is undesirable may be present such as HCN or NH3. It is often necessary for the intended purposes of the gas stream to remove these compounds at least partly, for example to prevent catalyst poisoning in processes after the gasification stage. Processes for the removal of sulphur compounds are known in the art.

In EP 324,526 a process is described for the removal of H₂S, COS, CS₂ and S0₂ from a gas stream, by converting COS and CS into H₂S. Although EP 324,526 mentions the removal of H S, it does not specify the preferred type of process for H₂S removal, nor is the concentration of H₂S in the treated gas stream mentioned.

A process known in the art for the removal of H S from a gas stream is the partial oxidation of H S to S0 according to:

(1) Partial H S oxidation 2H S + 30₂ - 2H 0 + 2S0₂ The S0₂ formed can be (catalytically) converted to elemental sulphur according to the Claus reaction: (2) Claus reaction 4H₂S + 2S0 <-> 4H 0 + 3S This process is known as the Claus process. The Claus process is frequently employed both in refineries and for the processing of H S recovered from natural gas.

A disadvantage of the Claus process is that it is thermodynamically limited by the increase of the water vapour content and simultaneously by the decrease of the H S and S0 concentration as the H S conversion proceeds, with the result that the equilibrium of the Claus reaction shifts to the left. Since the dew point of water lies below the solidification point of sulphur, condensation of the water vapour in the process gas to remove this limitation can lead to serious problems, such as clogging due to the solidi ication of sulphur and corrosion due to the formation of sulfuric acid, causing serious operational problems.

At relatively low concentrations of H S, typically concentrations below 20 vol%, the Claus process is difficult to operate and requires special technical provisions.

Another disadvantage of the Claus process is that the concentration of H S in the treated gas is still relatively high. The Claus process has been improved to an extent where the H S content of the treated gas can be lowered to approximately 1 vol% (Superclaus-99 process) and the S0₂ content to approximately 0.02 vol%. However, especially in the case where it is necessary to comply with requirements with regard to residential use or environmental regulations with respect to emission of sulphur compounds, even lower concentrations of H S and S0₂, in the ppm range, have to be achieved. A disadvantage of the Claus and Superclaus process is that such low concentrations of H₂S and S0₂ cannot be achieved. The removal of HCN from gas streams is important not only because of its own toxic properties, but also in view of corrosive N0_X compounds which can evolve when both HCN and oxygen are present in a gas stream. In addition, HCN itself is corrosive to equipment when allowed to concentrate in liquid streams upon gas treating.

We have now found a relatively simple and inexpensive process for removing S0 , H S and HCN and optionally COS, CS₂ and NH₃ from a gas stream. In the process according to the invention, a combination of reaction steps is used to achieve the removal of sulphur compounds such as H S and S0 , and optionally also COS and/or CS₂, as well as HCN from a gas stream comprising these compounds, to concentrations of below 10 ppmv for H S, below 100 ppmv for S0₂ and below 0.01 vol%, preferably 10 ppmv for HCN. The invention relates to a process for the removal of S0 , HCN and H₂S and optionally one or more compounds from the group of COS, CΞ and NH₃ from a first gas stream, which process comprises the steps of: (a) removing S0 from the first gas stream by contacting the first gas stream in a hydrogenation zone with a hydrogenation catalyst in the presence of hydrogen to obtain a second gas stream; (b) removing HCN and optionally COS and/or CS₂ from the second gas stream obtained in step (a) by contacting the second gas stream in a hydrolysis zone with a hydrolysis catalyst in the presence of water to obtain a third gas stream;

(c) removing NH₃ from the third gas stream by contacting the third gas stream in a NH₃-removal zone with an aqueous (acidic) washing liquid to obtain an ammonium-comprising aqueous stream and a fourth gas stream;

(d) removing H₂S from the fourth gas stream by contacting the fourth gas stream in a H₂S-removal zone with an aqueous alkaline washing liquid to obtain a H S- depleted gas stream and a hydrogen-sulphide-comprismg aqueous stream;

(e) contacting the hydrogen-sulphide-compπsing aqueous stream obtained m step (d) with sulphide-oxidizing bacteria in the presence of oxygen in a oxidation reactor to obtain a sulphur slurry and a regenerated aqueous alkaline washing liquid;

(f) separating at least part of the sulphur slurry obtained in step (e) from the regenerated aqueous alkaline washing liquid and;

(g) recycling regenerated aqueous alkaline washing liquid obtained in step (e) to the H S-removal zone in step (d) .

In step (a) of the process according to the invention, S0₂ is removed from the first gas stream by contacting the first gas stream in a hydrogenation zone with a hydrogenation catalyst in the presence of hydrogen to obtain a second gas stream. In the hydrogenation zone, S0₂ is converted to H₂S according to reaction (3) : (3) Hydrogenation reaction S0₂ + 3H → H₂S + 2H₂0 Reference herein to a first gas stream is to a gas stream comprising H₂S, S0₂, HCN and optionally one or more compounds selected from the group of COS, CS and NH3. The process is especially suitable for first gas streams having a total concentration of sulphur compounds, especially a total concentration of H₂S, of between 10 ppmv and 30 vol%, preferably between 100 ppmv and 20 vol%, based on the total gas stream. At these relatively low concentrations of sulphur, especially of H₂S, conventional processes such as the Claus process cannot be operated without additional technical provisions, for example amine treatment, to concentrate the H S content, whereas the process according to the invention can be operated without the need for additional technical provisions Typically, the amount of H S in the first gas stream is at least 50% of the sulphur compounds, preferably 80%, more preferably 90%.

Usually, the total concentration of HCN in the first gas stream is typically between 10 and 5000 ppmv, suitably between 20 and 1000 ppmv, or between 40 and 250 ppmv, based on the total gas stream. Optionally, solid compounds present in the first gas stream can be removed from the first gas stream prior to entering the hydrogenation zone, for example by use of a filter. This results in less contamination of the sulphur product in step (e) of the process. The hydrogenation zone can be a gas/solid contactor, preferably a fixed bed reactor. Suitable hydrogenation catalysts are for example cobalt/molybdenum, cobalt/tungsten or nickel/molybdenum catalysts. The hydrogenation catalysts suitable for the process according to the invention can be supported, preferably on a refractory oxide support, more preferably on an alumina support. Suitably, the temperature in the hydrogenation zone is between 200 °C and 380 °C, preferably between 210 °C and 360 °C, more preferably between 250 °C and 350 °C, still more preferably between 280 and 330 °C. It is found that the hydrogenation reaction proceeds at favourable rates at these temperature ranges. At a temperature range of between 280 and 330 °C, the highest reduction of S0 is achieved. The pressure in the hydrogenation zone is suitably between 1 and 100 bara, preferably between 2 and 80 bara.

The hydrogenation reaction results in the second gas stream having a concentration of S0 below 100 ppmv, preferably between 0.001 ppmv and 100 ppmv, more preferably between 0.01 ppmv and 50 ppmv, suitably between 0.1 ppmv and 15 ppmv, especially between 0.5 ppmv and 10 ppmv, based on the total gas stream.

In step (b) of the process according to the invention, HCN and optionally COS and/or CS are removed from the second gas stream obtained in step (a) by contacting the second gas stream in a hydrolysis zone with a hydrolysis catalyst to obtain a third gas stream. In the hydrolysis zone, HCN and, if applicable, COS and/or CS₂ are converted according to the following reactions: (4) Hydrolysis of HCN HCN + H 0 -. NH₃ + CO

(5) Hydrolysis of COS COS + H 0 → H₂S + C0₂

(6) Hydrolysis of CS CS₂ + 2H 0 - 2H S + C0₂ The amount of water/steam in the hydrolysis zone is preferably between 10 v/v% and 80 v/v%, more preferably between 20 v/v% and 70 v/v%, still more preferably between 30 v/v% and 50 v/v%, based on steam. At the preferred water/steam amounts, the conversion of HCN and optionally COS and/or CS₂ is better. Typically, the amount of H₂0 in the gas stream is sufficient to achieve conversion of HCN optionally COS and/or CS₂. Optionally, water or steam of a mixture thereof may be added to the second gas stream prior to contacting the second gas stream with the hydrogenation catalyst, in order to achieve the desired water/steam amount. Optionally, the reaction conditions are selected in such a way, that the reaction mixture remains below the dewpomt of H₂0. The H 0 in the gas stream can then advantageously be used for the conversion of HCN and optionally COS and/or CS₂ to the desired levels.

If COS and/or CS are present, the total concentration of COS and CS in the second gas stream is suitably between 10 ppmv and 2 vol%, preferably between 20 ppmv and 1 vol%, based on the total gas stream.

The hydrolysis zone can be a gas/solid contactor, preferably a fixed bed reactor.

Catalysts for the hydrolysis of HCN and optionally COS and/or CS₂ are known to those skilled in the art and include for example Tι0₂-based catalysts or catalysts based on alumina and/or chromium-oxide. Preferred catalysts are Tι0₂-based catalysts.

Optionally, the hydrolysis step can be done prior to the hydrogenation step. A disadvantage of performing the hydrogenation step prior to the hydrolysis step is that when a Tι0₂ catalyst is used, the Tι0₂ catalyst can also catalyze the Claus reaction, leading to the formation of sulphur from H₂S and S0₂. However, in the case where the temperature is above the dew point of sulphur, the formation of sulphur from the Claus reaction does not lead to clogging. The hydrolysis results in a third gas stream having a concentration of HCN below 0.01 vol%, suitably between 0.1 ppmv and 0.01 vol%, preferably between 1 ppmv and 50 ppmv, based on the total gas stream. The concentration of COS, if present, in the third gas stream is below 0.01 vol%, suitably between 10 ppmv and 0.01 vol%, preferably between 15 ppmv and 100 ppmv, based on the total gas stream.

The concentration of CS₂, if present, in the third gas stream is below 0.01 vol%, suitably between 1 ppmv and 0.01 vol%, preferably between 2 ppmv and 50 ppmv, based on the total gas stream.

In step (c) of the process according to the invention NH₃ is removed from the third gas stream by contacting the third gas stream in an NH₃-removal zone with an aqueous (acidic) washing liquid to obtain an ammonium-comprising aqueous stream and a fourth gas stream. The process is especially suitable for a third gas stream having an amount of NH₃ of between 10 and 6000 ppmv, preferably between 20 and 2000 ppmv. The temperature in the NH₃-removal zone is suitably between 5 and 70 °C, preferably between 10 and 50 °C, to achieve a sufficient removal of NH₃ at a low temperature. The pressure in the NH₃-removal zone is suitably between 1 and 100 bara, preferably between 2 and 80 bara, to achieve a sufficient removal of NH₃ at a low pressure.

In step (d) of the process according to the invention H₂S is removed from the fourth gas stream by contacting the fourth gas stream in H S-removal zone with an aqueous alkaline washing liquid to obtain a H₂S-depleted gas stream and a hydrogen-sulphide-comprising aqueous stream. The process is especially suitable if the load of sulphur compounds m the H₂S-removal zone is below 60000 kg/day, suitably between 50 and 50000 kg/day, preferably between 75 and 20000 kg/day, more preferably between 100 and 10000 kg/day. At these sulphur loads, conventional processes such as the Claus process are difficult, if not impossible, to operate, whereas the process according to the invention can be used advantageously.

Suitably, the total amount of H₂S of the fourth gas stream is between 10 ppmv and 20 vol%, preferably between 20 ppmv and 10 vol%. An advantage of the process according to the invention is that the H S in the fourth gas stream can be removed even when the H₂S amount is relatively low, typically between 10 ppmv and 20 vol% . For other processes such as the Claus process it is necessary that a sour gas is produced that has a high H₂S content to make it suitable as a Claus feed, for example by an amine treatment and regeneration step prior to the Claus reaction. Suitable aqueous washing liquids include aqueous hydroxide solutions, e.g. sodium hydroxide or potassium hydroxide solutions in water. The pH of the aqueous alkaline solvents is suitably between 7 and 12, preferably between 8 and 11. The main reactions that can take place in the

H₂S-removal zone in step (d) are:

(7) H₂S absorption H₂S + OH" -→ HS^" + H₂0

(8) H₂S absorption H S + C0₃ ^2- → HS^" + HC0₃ ^"

(9) C0₂ absorption C0₂ + OH" → HC0₃ ^" (10) Carbonate formation HC0₃ ^_ + OH- → C0₃ ²~+ H₂0 (11) Poly-hydrosulphide 2HS^" + SQ → 2HS5" formation

The term sulphide-comprising aqueous stream as used herein refers to an aqueous stream comprising one or more products of the main reactions (7) to (11) that can take place in the H S-removal zone, such as HS", d sulphides, polysulphides, thiocarbonates and carbonates but can also include dissolved H₂S.

The preferred temperature in the H₂S removal zone is between 5 and 70 °C, more preferably between 10 and 50 °C. Preferably, the pressure in the H₂S removal zone is between 1 and 100 bara, more preferably between 2 and 80 bara.

Typically, the H₂S removal zone is a gas/liquid contactor. Suitable gas/liquid contactors are described in Perry's Chemical Engineers' Handbook, 7^t'¹ edition, section 14 (1997) and include for example a tray or packed column or a gas scrubber.

Optionally, the medium of the H₂S removal zone is buffered. Preferred buffering compounds are carbonates, bicarbonates phosphates and mixtures thereof, especially sodium carbonate and/or sodium bicarbonate. The concentration of the buffering compounds depends inter alia on the composition of the gas flow and is generally adjusted in such a way, that the pH of the reaction medium in the H S removal zone is between 6.0 and 10, more preferably between 6.5 and 9.0.

Optionally, fresh alkaline washing liquid can be supplied to the H₂S removal zone to achieve the desired pH. Due to their odorous nature, H₂S, mercaptans, sulphides, disulphides and aromatic mercaptans can be detected at parts per million concentrations. Thus, it is desirable for users of such gas and refinery streams to have total concentration of sulphur compounds, especially H₂S, lowered to a concentration of e g. less than 30 or 20 ppmv, preferably less than 10 ppmv, based on the total H S-depleted gas stream

The process results in a "H₂S-depleted gas stream" having a total concentration of sulphur compounds, especially H₂S, of below 35 ppmv, suitably between 0.01 and 30 ppmv, or below 25 ppmv, suitably between 0 01 and 20 ppmv, or below 15 ppmv, suitably between 0.01 and 10 ppmv, preferably between 0 05 and 3.5 ppmv, more preferably between 0.1 and 1 ppmv, based on the total gas stream.

In step (e) of the process according to the invention the hydrogen-sulphide-comprising aqueous stream obtained in step (d) is contacted with sulphide-oxidizing bacteria in the presence of oxygen in a oxidation reactor to obtain a sulphur slurry and a regenerated aqueous alkaline washing liquid. The main reaction that can take place in the oxidation reactor in step (e) is the microbiological formation of sulphur and sulphate:

(12) Sulphur production HS" + H 0₂ → 1/8 Sg + OH"

(13) Sulfate production HS~ + 20₂ + OH" → S0 ^2- + H₂0 The term sulphur slurry as used herein refers to a slurry comprising one or more products of the main reactions, including reactions (12) and (13), that can take place in the oxidation reactor.

The term regenerated aqueous alkaline solvent as used herein refers to an aqueous alkaline solvent wherein at most 2 w/w% sulphur particles are present, preferably at most 1 w/w% The amount of oxygen fed into the oxidation reactor is adjusted such that the oxidation of absorbed sulphide results predominantly in sulphur, as suggested in NL 8801009, disclosing a process for the controlled oxidation of sulphur-containing waste water

Reference herein to sulphide-oxidizing bacteria is to bacteria which can oxidize sulphide to elemental sulphur. Suitable sulphide-oxidizing bacteria can be selected for instance from the known auto tropic aerobic cultures of the genera Thiobacillus and Thiomicrospira.

Typical pressures in the oxidation reactor in step (e) are between 1 and 2 bara.

Suitably, the oxidation reactor has a volume of between 5 and 2500 m^, preferably between 10 and 2000 m^. Preferably, the reaction medium in the oxidation reactor in step (e) is buffered The buffering compounds are chosen in such a way that the bacteria present in the oxidation reactor tolerate them. Preferred buffering compounds are carbonates, bicarbonates phosphates and mixtures thereof, especially sodium carbonate and/or sodium bicarbonate. The concentration of the buffering compounds depends inter alia on the composition of the gas flow and is generally adjusted in such a way, that the pH of the reaction medium n the oxidation reactor is between 6 and 10, more preferably between 7 and 9.

In step (f) of the process according to the invention at least part, typically between 5 and 95 w/w%, preferably between 10 and 90 w/w% based on the total weight of the slurry, of the sulphur slurry obtained in step (e) is separated from the regenerated aqueous alkaline solvent. The phrase "at least part of" as used herein also includes a complete separation of sulphur from the regenerated aqueous alkaline liquid. Suitably, the separating step takes place in a solid/liquid separator. Suitable solid/liquid separators are described in Perry's Chemical Engineers' Handbook, 7^th edition, section 22 (1997). Typically, the sulphur content of the separated aqueous sulphur slurry is between 5 w/w% and 50 w/w%, based on the slurry. Typically, the water of the sulphur slurry is removed to an extent that a sulphur cake with a dry solids content of between 55 and 70% is obtained. Typically, the sulphur content of the sulphur cake is between 90 and 98 w/w%, based on the total weight of the sulphur cake. Optionally, the sulphur slurry obtained in step (c) can be re-slurried, filtered and dried to obtain a sulphur paste w th a purity of at least 95 wt% sulphur, preferably at least 99 wt% sulphur. The sulphur paste thus-obtained can optionally be dried to produce a powder with a dry weight content of at least 85%, preferably at least 90%. This powder can suitably be applied as a fungicide or as a miticide. The sulphur produced in the process according to the invention has a hydrophilic nature and does not cause the fouling problems that are typically caused by sulphur produced by non-biological liquid processes. Another advantage of the sulphur produced in the process according to the invention is that it is very suitable for use as a fertilizer.

In step (g) of the process according to the invention, regenerated aqueous alkaline washing liquid obtained in step (e) is recycled to the H₂S-removal zone in step (d) . Suitably, between 10 and 99%, preferably between 30 and 95%, more preferably between 40 and 90% of the total amount of regenerated aqueous alkaline washing liquid obtained in step (e) is recycled to the H₂S-removal zone in step (d) . By recycling the regenerated aqueous washing liquid to the H₂S-removal zone fresh aqueous washing liquid is supplied to the H₂S-removal zone for the removal of H₂S. This enhances the removal of H₂S to a concentration of 30 ppmv or less, suitably 20 ppmv or less, preferably 10 ppmv or less. The regenerated aqueous alkaline washing liquid optionally comprises sulphur particles.

The process according to the invention is especially suitable for the treatment of a gaseous CO-containing stream, especially a syngas stream, an offgas stream from a carbon black plant, or a refinery gas stream. Syngas is a general term that is applied to mixtures of carbon monoxide, hydrogen, inert components and, carbon dioxide that are derived from the gasification of coal, oil residues, waste or biomass. The main components of syngas are hydrogen and carbon monoxide. Further, often carbon dioxide and traces of methane are present. Refinery streams concern crude oil derived gaseous streams containing smaller or larger amounts of sulphur compounds. Recycle streams and bleed streams of hydrotreatment processes, especially hydrodesulfurisation processes, can also suitably be treated by the process according to the invention. The invention will now be illustrated by means of schematic figure 1. Figure 1 depicts a typical process scheme according to the invention, wherein a gas stream comprising S0₂, HCN, H₂S and optionally COS, CS₂ and NH₃ enters via line (1) the hydrogenation zone (2) via line (1) and is contacted with the hydrogenation catalyst to remove the S0₂. Hydrogen is supplied to the hydrogenation zone via line (3) . After treatment in the hydrogenation zone the second gas stream, which is S0₂-depleted, leaves the hydrogenation zone via line (4) and enters the hydrolysis zone (5) where it is contacted with a hydrolysis catalyst to remove HCN and optionally COS and/or CS₂. Optionally, steam or a steam/water mixture can be added to the hydrolysis zone via line (6). After treatment in the hydrolysis zone, the third gas stream, which is depleted of HCN, COS and/or CS₂, leaves the hydrolysis zone via line (7) and enters the HN₃- removal zone (8), where it is treated with aqueous (acidic) washing liquid to obtain an ammonium-comprising aqueous stream and a fourth gas stream. Optionally, steam or a steam/water mixture can be added to the HN₃-removal zone via line (9) . After treatment in the NH₃-removal zone, the fourth gas stream, which is depleted of HCN, COS and/or CS₂ and NH₃, leaves the HN3-removal zone via line (10) and enters the H₂Ξ-removal zone (11) , where it is contacted with an aqueous washing liquid. The H₂S- depleted gas stream is led from the H₂S-removal zone via line (12), optionally via a knockout vessel (13) and can be further processed via line (14). A sulphide-comprising aqueous stream leaves the H S-removal zone via line (15) and enters a flash vessel (16) . H₂S-depleted excess gas is vented off from the flash vessel through line (17) . In the case that flash gas contains some H₂S, the H S is removed in a small flash gas contactor before further use as fuel gas. The sulphide-comprising aqueous stream is led via line (18) to the aerobic reactor (19) where the sulphide compounds are oxidized. Nutrients and air are fed to the aerobic reactor via feed lines (20) and (21) . The sulphur-containing sol d/lιquιd mixture generated in the aerobic reactor is led via line (22) to a solid/liquid separator (23) where the sulphur-slurry is separated and discharged via line (24). The liquid is led back to the bioreactor via line (25) . Off-gas is vented from the aerobic reactor via line (26) . The regenerated aqueous alkaline solvent is led to the H₂S-removal zone via line (27) .

The invention will now be illustrated by the following non-limiting examples. EXAMPLE 1 (comparative)

A gas stream containing sulphur- compounds and HCN with concentrations as given in table 1 is heated to a temperature of 280 °C and led to a reactor filled with a stacked bed of hydrogenation catalyst and hydrolysis catalyst. The gas is cooled in a quench tower at 40 °C and treated in an amme/Claus unit to remove the H₂S. The concentrations of sulphur compounds and of HCN in the treated gas is given in table 1.

Table 1

EXAMPLE 2 (according to the invention)

A first gas stream containing sulphur- compounds, NH₃ and HCN with concentrations as given in table 2 is heated to a temperature of 280 °C and led to a reactor filled with a stacked bed of hydrogenation catalyst and hydrolysis catalyst to create a second gas stream and subsequently a third gas stream. The third gas stream is cooled in a quench tower at 40 °C and treated in an NH3- scrubber to create a fourth gas stream. The fourth gas stream is treated in a H₂S-removal unit to create a H₂S- depleted gas stream. The resulting hydrogensulphides are oxidised in a bioreactor. The concentrations of the sulphur-containing compounds and of the HCN in the treated gas (H S-depleted gas) are given in table 2.

Table 2

From the examples it is clear that with the process according to the invention a substantially lower concentration of sulphur-containing compounds, especially of H S, S0₂, CS₂ and COS is achieved, while the concentration of NH3 and HCN is also lowered.

Claims

C L A I M S

1. A process for the removal of S0₂, HCN and H S and optionally one or more compounds from the group of COS, CS₂ and NH3 from a first gas stream, which process comprises the steps of. (a) removing S0₂ from the first gas stream by contacting the first gas stream in a hydrogenation zone with a hydrogenation catalyst in the presence of hydrogen to obtain a second gas stream,

(b) removing HCN and optionally COS and/or CS from the second gas stream obtained in step (a) by contacting the second gas stream in a hydrolysis zone with a hydrolysis catalyst in the presence of water to obtain a third gas stream;

(c) removing NH3 from the third gas stream by contacting the third gas stream in a NH3~removal zone with an aqueous acidic washing liquid to obtain an ammonium- comprising aqueous stream and a fourth gas stream;

(d) removing H S from the fourth gas stream by contacting the fourth gas stream in a H₂S-removal zone with an aqueous alkaline washing liquid to obtain a H S-depleted gas stream and a hydrogensulphide-comprising aqueous stream;

(e) contacting the hydrogensulphide-comprising aqueous stream obtained in step (d) with sulphide-oxidizing bacteria in the presence of oxygen in an oxidation reactor to obtain a sulphur slurry and a regenerated aqueous alkaline washing liquid; (f) separating at least part of the sulphur slurry obtained in step (e) from the regenerated aqueous alkaline washing liquid and;

(g) recycling regenerated aqueous alkaline washing liquid obtained in step (e) to the H₂S-removal zone in step (d) .

2. A process according to claim 1, wherein the sulphur- load m the H S-removal zone in step (d) is between 50 and 50000 kg/day, preferably between 75 and 20000 kg/day, more preferably between 100 and 10000 kg/day.

3. A process according to claim 1 or 2, wherein the total concentration of sulphur- compounds in the treated gas is below 30 ppmv, preferably between 0.01 and 20 ppmv.

4. A process according to any one of claims 1 to 3, wherein the total concentration of H₂S is below 30 ppmv, preferably between 0.01 and 20 ppmv.

5. A process according to any of claims 1 to 4, wherein the washing liquid in step (d) is buffered, preferably at a pH of between 6 and 10, more preferably at a pH between 6.5 and 9.

6 A process according to any of claims 1 to 5, wherein the contents of the oxidation reactor in step (e) is buffered, preferably at a pH between 6 and 10, more preferably between 7 and 9.

7. A process according to any of claims 1 to 6, wherein the oxidation reactor in step (e) has a volume of between

5 and 2500 m³.

8. A process according to any of claims 1 to 7, wherein the sulphur slurry obtained in step (e) is re-slurried, filtered and dried to obtain a sulphur-content of at least 95 wt%, preferably at least 99 wt%.

9. A process according to any of claims 1 to 8, wherein water or steam or a mixture thereof is added to the

second gas stream prior to contacting the first gas stream in a hydrolysis zone with a hydrolysis catalyst in step (b) .

10. A process according to any one of claims 1 to 9, wherein the water/steam content of the second gas stream is between 10 v/v% and 80 v/v%, preferably between

20 v/v% and 70 v/v%, more preferably between 30 v/v% and

50 v/v%, based on steam% .