WO2009027491A1

WO2009027491A1 - Process for removal of hydrogen sulphide and carbon dioxide from an acid gas stream

Info

Publication number: WO2009027491A1
Application number: PCT/EP2008/061355
Authority: WO
Inventors: Theodorus Johannes Brok; Gerardus Petrus Van Der Zwet
Original assignee: Shell Internationale Research Maatschappij BV
Current assignee: Shell Internationale Research Maatschappij BV
Priority date: 2007-08-30
Filing date: 2008-08-29
Publication date: 2009-03-05
Anticipated expiration: 2010-02-28
Also published as: US8765086B2; AU2008292143B2; JP2010536573A; US20100310439A1; EP2188040A1; CA2697944A1; CN101820975A; AU2008292143A1; ZA201001545B

Abstract

A process for removal of H2S and CO2 from an acid gas stream comprising H2S and CO2, the process comprising the steps of : (a) reacting H2S in the acid gas stream with SO2 to form sulphur vapour and water vapour, thereby obtaining a first off-gas stream comprising CO2, water vapour, sulphur vapour, residual SO2 and residual H2S; (b) converting residual SO2 in the first off-gas stream to H2S in a first off-gas treating reactor, thereby obtaining a second off-gas stream depleted in SO2 and enriched in H2S and CO2 compared to the first off-gas stream; (c) contacting the second off-gas stream with an H2S absorbing liquid, thereby transferring H2S from the gas stream to the H2S absorbing liquid to obtain H2S absorbing liquid enriched in H2S and a third off-gas stream enriched in CO2; (d) removing CO2 from the third off-gas stream by contacting the third off-gas stream with CO2 absorbing liquid in a CO2 absorber, thereby transferring CO2 from the third off-gas stream to the CO2 absorbing liquid to obtain CO2 absorbing liquid enriched in CO2 and purified gas.

Description

PROCESS FOR REMOVAL OF HYDROGEN SULPHIDE AND CARBON DIOXIDE FROM AN ACID GAS STREAM

The invention relates to a process for removal of hydrogen sulphide (H2S) and carbon dioxide (CO2) from an acid gas stream.

A process known in the art for removal of H2S from a gas stream uses the partial oxidation of H2S to SO2 according to:

2 H₂S + 3O₂ → 2H₂O + 2SO₂ (1)

The SO₂ formed can be ( catalytically) converted to elemental sulphur according to the Claus reaction: 2 H₂S + SO₂ → 2H₂O + 3/n S_n (2)

The combination of reactions (1) and (2) is known as the Claus process. The Claus process is frequently employed both in refineries and for the processing of H₂S recovered from natural gas . The Claus process results in a gas still comprising unreacted H₂S and/or SO₂. Increasingly rigorous standards concerning the protection of the environment make simple venting or incineration of the final gas stream an unattractive or impermissible choice. Thus, the Claus tail gas is generally passed to a tail gas clean up unit, which is able to effectively remove H₂S or SO₂, notwithstanding their low concentration. A number of commercially available tail gas clean up processes are known in the art. For example, in US 6,962,680 a process is described for removing sulphur compounds from a gas comprising besides H₂S also a substantial amount of carbon dioxide. The gas is separated into a concentrated gas containing H₂S and a residual gas containing carbon dioxide, mercaptans and aromatic compounds. The concentrated gas is transferred to a Claus reaction process in which the H2S is recovered as elemental sulphur. Off-gas discharged from the Claus reaction is heated and mixed with the residual gas; the resultant mixture is transferred to a hydrogenation reactor where residual sulphur compounds are converted to H2S. Thus- formed H2S is separated using an absorption-regeneration step. Gas exiting the regeneration step is returned to the Claus reaction. A disadvantage of the process described in US 6,962,680 is that the gas leaving the regeneration tower, which contains besides hydrogen sulphide also a substantial amount of carbon dioxide, is returned to the Claus sulphur recovery unit. This results in dilution of the Claus feed gas and a lower rate of the Claus reaction.

Furthermore, the process described in US 6,962,680 results in a considerable emission of carbon dioxide into the atmosphere from the absorption step. During the last decades there has been a substantial global increase in the amount of CO2 emission to the atmosphere. Following the Kyoto agreement, CO2 emission has to be reduced in order to prevent or counteract unwanted changes in climate . Thus, there remains a need in the art for a process enabling removal of H2S and CO2 from an acid gas stream comprising H2S and CO2, both in considerable amounts, wherein emission of CO2 into the atmosphere is reduced to a minimum. To this end, the invention provides a process for removal of H2S and CO2 from an acid gas stream comprising

H2S and CO2, the process comprising the steps of: (a) reacting H2S in the acid gas stream with SO2 to form sulphur vapour and water vapour, thereby obtaining a first off-gas stream comprising CO2, water vapour, sulphur vapour, residual SO2 and residual H2S; (b) converting residual SO2 in the first off-gas stream to H2S in a first off-gas treating reactor, thereby obtaining a second off-gas stream depleted in SO2 and enriched in H2S and CO2 compared to the first off-gas stream; (c) contacting the second off-gas stream with an H2S absorbing liquid, thereby transferring H2S from the gas stream to the H2S absorbing liquid to obtain H2S absorbing liquid enriched in H2S and a third off-gas stream enriched in CO2; (d) removing CO2 from the third off-gas stream by contacting the third off-gas stream with CO2 absorbing liquid in a CO2 absorber, thereby transferring CO2 from the third off-gas stream to the CO2 absorbing liquid to obtain CO2 absorbing liquid enriched in CO2 and purified gas.

The purified gas, having very low concentrations of contaminants, especially CO2, may be vented into the atmosphere in compliance with environmental standards . In addition, CO2 may be recovered from the CO2 absorbing liquid enriched in CO2, optionally pressurised and used for example in enhanced oil recovery.

The process according to the invention is especially suitable for acid gas streams comprising significant amounts of CO2 in addition to H2S, as both compounds are efficiently removed. Suitably, the acid gas stream comprises in the range of from 5 to 95 vol%, preferably from 40 to 95 vol%, more preferably from 60 to 95 vol% of H2S, based on the total acid gas stream. Suitably, the acid gas stream comprises at least

1 vol%, preferably at least 5 vol%, more preferably at least 10 vol% of CO2, based on the total acid gas stream.

These amounts of CO2 in the acid gas stream will translate into comparable amounts of CO2 in the third off-gas stream.

Preferably, the acid gas stream is obtained from the regeneration step of a gas purification process. A gas purification process is required in order to reduce the concentration of especially H2S in industrial gases such as refinery gas, natural gas or synthesis gas, and generally involves absorbing H2S in liquid absorbent, which is subsequently regenerated to give H2S-rich gases.

In step (a), H2S in the acid gas stream is reacted with SO2 to form sulphur vapour and water vapour, thereby obtaining a first off-gas stream comprising CO2, water vapour, sulphur vapour, residual SO2 and residual H2S.

Suitably, step (a) takes place in a Claus unit. In the Claus unit, part of the H2S in the acid gas is partially oxidised using oxygen-containing gas (including pure oxygen) to form SO2, followed by reaction of the SO2 formed with the remaining part of the H2S in the presence of a Claus catalyst, preferably non-promoted spherical activated alumina.

The Claus unit suitably comprises a combustion chamber followed by two or more catalyst beds and two or more condensers. The reaction products are cooled in these condensers and liquid elemental sulphur is recovered. Since the yield of elemental sulphur is not quantitative, a minor amount of unreacted hydrogen sulphide and unreacted sulphur dioxide remains in the off-gases from the Claus unit. The off-gas from the Claus unit, which is the first off-gas stream, therefore still comprises residual SO2 and residual H2S. As the partial oxidation of H2S to SO2 usually is done with air as oxygen-containing gas, a substantial amount of nitrogen will be present in all gas streams exiting the Claus unit. Thus, the first off-gas stream will also comprise a substantial amount of nitrogen besides the aforementioned components .

In step (b) , the first off-gas stream is passed to a first off-gas treating reactor to remove residual SO2. In the first off-gas treating reactor SO2 is reduced to H2S in a hydrogenation reaction. Further, COS (if present) is converted to H2S.

A preferred off-gas treating reactor is a so-called SCOT reactor, i.e., Shell Claus Off-gas Treating reactor, as for example described in the well-known textbook by

Kohl and Riesenfeld, Gas Purification, 3^rc^ ed. Gulf Publishing Co, Houston, 1979.

The temperature in the first off-gas treating reactor is suitably in the range of from 150 to 450 ⁰C, preferably from 180 to 250 ⁰C. At a temperature above 180 ⁰C, the presence of small amounts of elemental sulphur in the form of mist in the reaction off-gas is avoided, as the temperature is now above the dew point of sulphur.

In the first off-gas treating reactor, preferably a Group VI and/or Group VII metal catalyst supported on an inorganic carrier is used. Preferably, the catalyst comprises at least one metal selected from the group consisting of copper, cobalt, chromium, vanadium and molybdenum. The metal is suitably present on the catalyst in the form of its oxide or sulphide. The carrier can be selected from the group consisting of alumina, silica, silica-alumina, titania, zirconia and magnesia.

A second off-gas stream, depleted in SO2 and enriched in H2S and CO2 compared to the first off-gas stream, is emitted from the first off-gas treating reactor. Suitably, the second off-gas stream comprises less than 500 ppmv H2S, preferably less than 200 ppmv, more less than 100 ppmv H2S, based on the total second off-gas stream.

It will be understood that the amount of CO2 in the second off-gas stream will depend on the amount of CO2 in the first off-gas stream. Suitably, the amount of CO2 in the second off-gas stream is in the range of 105 to 150% of the amount of CO2 in the first off-gas stream.

In step (c), the second off-gas stream is contacted with an H2S absorbing liquid, thereby transferring H2S from the gas stream to the H2S absorbing liquid to obtain H2S absorbing liquid enriched in H2S and a third off-gas stream enriched in CO2.

Prior to being contacted with the H2S absorbing liquid, the second off-gas stream is suitably cooled, preferably to a temperature in the range of from 6 to 60 ⁰C. More preferably, cooling is effected in two steps, the first one being an indirect heat exchange and the second one a direct heat exchange with water. A preferred H2S absorbing liquid comprises a chemical solvent and/or a physical solvent, suitably as an aqueous solution .

Suitable chemical solvents are primary, secondary and/or tertiary amines, including sterically hindered amines .

A preferred chemical solvent comprises a secondary or tertiary amine, preferably an amine compound derived from ethanol amine, more especially DIPA, DEA, MMEA (monomethyl-ethanolamine) , MDEA (methyldiethanolamine ) TEA (triethanolamine) , or DEMEA (diethyl- monoethanolamine) , preferably DIPA or MDEA. It is believed that these chemical solvents react with acidic compounds such as H2S. Step (c) is suitably performed in an absorption column, either a packed or a tray column may be used. In order to decrease the co-absorption of CO2 a relatively high gas velocity is applied. It is preferred to use a gas velocity in the range of from 1.0 to 3.0 m/s. It is further preferred to apply an absorption column having less than 20 absorption layers. For example, when using a tray column in step (c), the tray column preferably has less than 20 contacting valve trays. When using a packed column in step (c), the packed column preferably has less than 20 theoretical plates. The use of an absorption zone having between 5 and 15 absorption layers is particularly preferred in step (c) .

After passage through the H2S absorbing liquid in step (c), the unabsorbed part of the second off-gas stream, which now comprises a substantial amount of CO2 is discharged from the H2S absorption column as a third off-gas stream. The invention is especially suitable in the event that the third off-gas stream comprises a relatively large amount of CO2, preferably at least 1 vol%, more preferably at least 5 vol%, still more preferably at least 10 vol% and most preferably at least 20 vol% of CO2, based on the total third off-gas stream.

It is an advantage of the process that the amount of sulphur compounds, especially SO2, is very low. This enables the use of standard carbon steel equipment for step (d) , whereas for known CO2 removal equipment, for example CO2 removal from flue gases, expensive stainless steel equipment has to be used.

Furthermore, there is no need for a quench column, as the gas has already been quenched in step (c). In step (d), CO2 is removed from the third off-gas stream by contacting the third off-gas stream with CO2 absorbing liquid in a CO2 absorber, thereby transferring CO2 from the third off-gas stream to the CO2 absorbing liquid to obtain CO2 absorbing liquid enriched in CO2 and purified gas.

Suitably, step (d) takes place at elevated pressure, and at relatively low temperature. Elevated pressure means that the operating pressure of the CO2 absorber is above ambient pressure. Preferably, step (d) takes place at an operating pressure in the range of from 20 to 200 mbarg, more preferably from 50 to 150 mbarg. As the third off-gas stream is already at elevated pressure, the pressure difference between the third off-gas stream pressure and the operating pressure of the CO2 absorber is relatively small. Thus, the third off-gas stream does not need to be pressurised or needs to be pressurised to a lesser extent prior to entering the CO2 absorber. Given the large volume of gas to be pressurised, the use of a smaller pressurising equipment or elimination of the need for pressurizing equipment altogether will result in a considerable cost-saving for the overall process. The CC>2 absorbing liquid may be any absorbing liquid capable of removing CO2 from a gas stream. Such CO2 absorbing liquids may include chemical and physical solvents or combinations of these.

Suitable physical solvents include dimethylether compounds of polyethylene glycol.

Suitable chemical solvents include ammonia and amine compounds .

In one embodiment, the CO2 absorbing liquid comprises one or more amines selected from the group of monethanolamine (MEA), diethanolamine (DEA), diglycolamine (DGA), methyldiethanolamine (MDEA) and triethanolamine (TEA) . MEA is an especially preferred amine, due to its ability to absorb a relatively high percentage of CO2 (volume CO2 per volume MEA) . Thus, an absorbing liquid comprising MEA is suitable to remove CO2 from third off-gas streams having low concentrations of CO2, typically 3-10 volume % CO2.

In another embodiment, the CO2 absorbing liquid comprises one or more amines selected from the group of methyldiethanolamine (MDEA), triethanolamine (TEA), N, N'- di (hydroxyalkyl) piperazine, N, N, N ' , N' - tetrakis (hydroxyalkyl) -1, 6-hexanediamine and tertiary alkylamine sulfonic acid compounds.

Preferably, the N, N ' -di (hydroxyalkyl) piperazine is N, N ' -d- ( 2-hydroxyethyl) piperazine and/or N,N'-di-(3- hydroxypropyl ) piperazine . Preferably, the tetrakis (hydroxyalkyl) -1, 6- hexanediamine is N, N, N' ,N'-tetrakis (2-hydroxyethyl) -1, 6- hexanediamine and/or N, N, N' , N' -tetrakis (2-hydroxypropyl) - 1, 6-hexanediamine . Preferably, the tertiary alkylamine sulfonic compounds are selected from the group of 4- (2- hydroxyethyl) -1-piperazineethanesulfonic acid, 4- (2- hydroxyethyl) -1-piperazinepropanesulfonic acid, 4- (2- hydroxyethyl) piperazine-1- ( 2-hydroxypropanesulfonic acid) and 1, 4-piperazinedi ( sulfonic acid).

In an especially preferred embodiment, the CO2 absorbing liquid comprises a combination of amines, the combination being one of more amines selected from the group of monethanolamine (MEA), diethanolamine (DEA), diglycolamine (DGA), methyldiethanolamine (MDEA) and triethanolamine (TEA) in combination with one of more amines selected from the group of N, N'- di (hydroxyalkyl) piperazine, N, N, N ' , N' - tetrakis (hydroxyalkyl) -1, 6-hexanediamine and tertiary alkylamine sulfonic acid compounds.

The CO2 absorbing liquid may further comprise N- ethyldiethanolamine (EDEA) and/or piperazine, especially in combination with one of more amines selected from the group of monethanolamine (MEA), diethanolamine (DEA), diglycolamine (DGA), methyldiethanolamine (MDEA) and triethanolamine (TEA) .

In another preferred embodiment, the CO2 absorbing liquid comprises ammonia.

Suitably, the amount of oxygen in the third off-gas stream is very low. Oxygen can cause amine degradation and can lead to the formation of degradation products in the absorbing liquid. A lower oxygen content of the third off-gas stream will therefore result in less amine degradation and less formation of degradation products.

In the event that the third off-gas stream comprises an appreciable quantity of oxygen, suitably in the range of from 1 to 20% (v/v) of oxygen, preferably a corrosion inhibitor is added to the absorbing liquid. Suitable corrosion inhibitors are described for example in US 6,036,888.

The purified gas obtained in step (d) comprises very little CC>2. Suitably, the purified gas comprises less than 0.5 vol%, preferably less than 0.1 vol% and more preferably less than 0.01 vol% of CO₂. The purified gas may be vented into the atmosphere of incinerated.

In most cases it will be desirable to have a continuous process, including regeneration of the CO2 absorbing liquid. Thus, preferably the process further comprises the step of regenerating the CO2 absorbing liquid enriched in CO2 by contacting the absorbing liquid enriched in CO2 with a stripping gas at elevated temperature in a regenerator to obtain regenerated absorbing liquid and a gas stream enriched in CO2. It will be understood that the conditions used for regeneration depend inter alia on the type of absorbing liquid and on the conditions used in the absorption step. Suitably, regeneration takes place at a different temperature and/or different pressure than the absorption .

In the event that the CO2 absorbing liquid comprises an amine, preferred regeneration temperatures are in the range of from 100 to 200 ⁰C. In the event that the CO₂ absorbing liquid comprises an aqueous amine, regeneration preferably takes place at pressure in the range of from 1 to 5 bara.

In the event that the CO2 absorbing liquid comprises ammonia, suitably the absorbing step is performed at temperatures below ambient temperature, preferably in the range of from 0 to 10 ⁰C, more preferably from 2 to 8 ⁰C.

The regeneration step is suitably performed at temperatures higher than used in the absorption step. When using a CO2 absorbing liquid comprising ammonia, the CC>2-enriched gas stream exiting the regenerator is at elevated pressure. Suitably, the pressure of the CO2- enriched gas stream is in the range of from 5 to 8 bara, preferably from 6 to 8 bara. In applications where the CO2~enriched gas stream needs to be at a high pressure, for example when it will be used for injection into a subterranean formation, it is an advantage that the CO2- enriched gas stream is already at an elevated pressure. Normally, a series of compressors is needed to pressurise the CC>2-enriched gas stream to the desired high pressures. A CO2~enriched gas stream which is already at elevated pressure is easier to further pressurise.

Preferably, the gas stream enriched in carbon dioxide is pressurised to produce a pressurised carbon dioxide stream. Preferably, the pressurised CO2 stream has a pressure in the range of from 40 to 300 bara, more preferably from 50 to 300 bara. A CO2 stream having a pressure in these preferred ranges can be used for many purposes, in particular for enhanced recovery of oil, coal bed methane or for sequestration in a subterranean formation.

Especially for purposes wherein the pressurised CO2 stream is injected into a subterranean formation, high pressures are required. In a preferred embodiment, the pressurised CO2 stream is used for enhanced oil recovery.

By injecting CO2 into an oil reservoir, the oil recovery rate can be increased. Typically, the pressurised CO2 stream is injected into the oil reservoir, where it will be mixed with some of the oil which is present. The mixture of CO2 and oil will displace oil which cannot be displaced by traditional injections.

Claims

C L A I M S

1. A process for removal of H2S and CO2 from an acid gas stream comprising H2S and CO2, the process comprising the steps of:

(a) reacting H2S in the acid gas stream with SO2 to form sulphur vapour and water vapour, thereby obtaining a first off-gas stream comprising CO2, water vapour, sulphur vapour, residual SO2 and residual H2S;

(b) converting residual SO2 in the first off-gas stream to H2S in a first off-gas treating reactor, thereby obtaining a second off-gas stream depleted in SO2 and enriched in H2S and CO2 compared to the first off-gas stream;

(c) contacting the second off-gas stream with an H2S absorbing liquid, thereby transferring H2S from the gas stream to the H2S absorbing liquid to obtain H2S absorbing liquid enriched in H2S and a third off-gas stream enriched in CO2;

(d) removing CO2 from the third off-gas stream by contacting the third off-gas stream with CO2 absorbing liquid in a CO2 absorber, thereby transferring CO2 from the third off-gas stream to the CO2 absorbing liquid to obtain CO2 absorbing liquid enriched in CO2 and purified gas .

2. A process according to claim 1, wherein the CO2 absorbing liquid comprises one or more amines, preferably selected from the group of monethanolamine (MEA) , diethanolamine (DEA), diglycolamine (DGA), methyldiethanolamine (MDEA) and triethanolamine (TEA) .

3. A process according to claim 1, wherein the CO2 absorbing liquid comprises a combination of amines, the combination being one of more amines selected from the group of monethanolamine (MEA), diethanolamine (DEA), diglycolamine (DGA), methyldiethanolamine (MDEA) and triethanolamine (TEA) in combination with one of more amines selected from the group of N, N'- di (hydroxyalkyl) piperazine, N, N, N ' , N' - tetrakis (hydroxyalkyl) -1, 6-hexanediamine and tertiary alkylamine sulfonic acid compounds.

4. A process according to claim 1, wherein the CO2 absorbing liquid comprises N-ethyldiethanolamine (EDEA) and/or piperazine, especially in combination with one of more amines selected from the group of monethanolamine (MEA), diethanolamine (DEA), diglycolamine (DGA), methyldiethanolamine (MDEA) and triethanolamine (TEA)

5. A process according to claim 1, wherein the CO2 absorbing liquid comprises ammonia.

6. A process according to any one of the preceding claims, wherein the feed acid gas stream is obtained by separating H2S and CO2 from a sour gas, preferably sour natural gas .

7. A process according to any one of the preceding claims, wherein the third off-gas stream comprises at least 1 vol%, preferably at least 5 vol%, more preferably at least 10 vol% of CO2, based on the total third off-gas stream.

8. A process according to any one of the preceding claims, the process further comprising the step of: (d) regenerating the absorbing liquid enriched in CO2 by contacting the absorbing liquid enriched in CO2 with a stripping gas at elevated temperature in a regenerator to obtain regenerated absorbing liquid and a gas stream enriched in CO2.

9. A process according to claim 8, the process further comprising the step of:

(d) pressurising the gas stream enriched in CO2.

10. A process according to claim 9, wherein the pressurised gas stream enriched in CO2 is used for enhanced oil recovery.