WO2013082242A1

WO2013082242A1 - Offshore gas separation process

Info

Publication number: WO2013082242A1
Application number: PCT/US2012/066986
Authority: WO
Inventors: Michel Daage; Richard A. Davi; Robert B. Fedich; Thomas F. PARKERTON; Michael Siskin
Original assignee: Exxonmobil Research And Engineering Company
Priority date: 2011-12-02
Filing date: 2012-11-29
Publication date: 2013-06-06
Also published as: CA2857632A1; EP2785437A1; US20130142717A1; RU2014125847A; CN104080525A

Abstract

A process for the selective absorption of normally gaseous acid components from hydrocarbon gas mixtures containing both the acidic components and gaseous non-acidic components which is carried out in a gas separation unit located at an offshore marine production installation. The sorbent used in the process comprises a severely sterically hindered amino ether. The process is capable of selectively removing H₂S from gas mixtures which also contain C0₂ in addition to the hydrocarbon components.

Description

Offshore Gas Separation Process

Field of the Invention

[0001] This invention relates to a process carried out on an offshore petroleum production platform for removing acid gases from gas produced at the platform. It also relates to the gas treatment unit for carrying out the process.

Background of the Invention

[0002] As reserves in onshore natural gas and petroleum fields have decreased over time, production of these resources has moved progressively offshore and recently into ever deeper waters. Interest in natural gas production has increased as the utility of this energy source in transport, electrical power generation and other applications have increased in recent years with recognition of the importance of reducing atmospheric carbon emissions. The natural gas produced with petroleum liquids and the gas from a gas field frequently contains carbon dioxide and sulfur in the form of hydrogen sulfide, as well as other acid gases such as, CS₂, HCN, COS and sulfur derivatives of light hydrocarbons (mercaptans etc). Hydrogen sulfide (H₂S) is desirably separated to meet pipeline specifications before the gas is sent ashore by underwater pipeline in view of its corrosive action on pipeline steels. Similarly, it is also desirable to remove the hydrogen sulfide from gas which is stored or processed at a production facility which is not linked to the shore by a pipeline. When H₂S is dissolved in water, it forms a weak acid which promotes pipeline corrosion The most common types of corrosion where H₂S is present consist of pitting, blistering, embrittlement, fatigue, and cracking. The severity of the corrosion due to H₂S is determined by factors such as oxygen and carbon dioxide (CO₂) levels, temperature, gas velocity, pH levels less than 6.5 (acidic), especially in he presence of salt water (conductive electrolyte), internal/external stresses, concentration (parts per million or partial pressure levels). The combination of CO₂ and H₂S is more corrosive than H₂S alone, and can be considered very corrosive when combined with even minute quantities of oxygen and for this reason, removal of both CO₂ and H₂S is considered desirable.

[0003] The removal of acid gases from the produced fluids on offshore platforms and production rigs raises significant problems. The main constraints for application on an offshore platform are space and weight limitations. Installing a complex system with numerous equipment and extensive utilities to support its operation is against the trend in the offshore industry to pursue compact facilities and to reduce manning levels for safety and logistic reasons and operating costs. A number of different technologies are available for consideration including, for example, chemical absorption (amine), physical absorption, cryogenic distillation (Ryan Holmes process), and membrane system separation. Of these, amine separation is a highly developed technology with a number of competing processes in hand using various amine sorbents such as monoethanolamine (MEA), diethanolamine (DEA), methyldiethanolamine (MDEA), diisopropylamine (DIPA), diglycolamine (DGA), 2- amino-2-methyl-1 -propanol (AMP) and piperazine (PZ). Of these, MEA, DEA, and MDEA are the ones most commonly used. The amine purification process usually contacts the gas mixture in the form of an aqueous solution of the amine in an absorber tower with the aqueous amine solution contacting the acidic fluid countercurrently. The liquid amine stream is then regenerated by desorption of the sorbed gases in a separate tower with the regenerated amine and the desorbed gases leaving the tower as separate streams. The various gas purification processes which are available are described, for example, in Gas Purification, Fifth Ed., Kohl and Neilsen, Gulf Publishing Company, 1997, ISBN-13: 978-0- 88415-220-0.

[0004] The treatment of acid gas mixtures containing CO₂ and H₂S with amine solutions typically results in the simultaneous removal of substantial amounts of both the CO₂ and H₂S. It is often desirable, however, to treat acid gas mixtures containing both CO₂ and H₂S so as to remove the H₂S selectively from the mixture, thereby minimizing removal of the CO₂. Selective removal of H₂S results in a relatively high H₂S/CO₂ ratio in the separated acid gas which simplifies the conversion of H₂S to elemental sulfur, e.g., using the Claus process. Although primary and secondary amines such as MEA, DEA, DPA, and DGA absorb both H₂S and CO₂ gas, they have not proven especially satisfactory for preferential absorption of H₂S. In aqueous solution, the amines undergo reaction with CO₂ to form carbamates. The tertiary amine, MDEA, has a high degree of selectivity toward H₂S absorption over CO₂ but the commercial usefulness of MDEA is limited because of its restricted capacity.

[0005] An improvement in the basic amine process involves the use of sterically hindered amines. U.S. Patent No. 4,1 12,052 describes the use of hindered amines for nearly complete removal of acid gases such as CO₂ and H₂S. U.S. Patents Nos. 4,405,581 ; 4,405,583; 4,405,585 and 4,471 ,138 disclose the use of severely sterically hindered amine compounds for the selective removal of H₂S in the presence of CO₂. Compared to aqueous MDEA, severely sterically hindered amines lead to much higher selectivity at high H₂S loadings. Amines described in these patents include BTEE (bis(tertiary-butylamino)-ethoxy- ethane synthesized from tertiary-butylamine and bis-(2-chloroethoxy)-ethane as well as EEETB (ethoxyethoxyethanol-tertiary-butylamine) synthesized from tertiary-butylamine and chloroethoxyethoxyethanol). U.S. 4,894, 178 indicates that a mixture of BTEE and EEETB is particularly effective for the selective separation of H₂S from CO₂. U.S. 2010/0037775 describes the preparation of alkoxy-substituted etheramines as selective sorbents for separating H₂S from CO_2. US 2009/0308248 describes a different class of absorbents which are selective for H₂S removal in the presence of CO₂, the hindered amino alkyl sulfonate, sulfate and phosphonate salts, with the sulfonate and phosphonates being the preferred species.

[0006] Regardless of the improved selectivities and sorption capacities offered by those new materials, they have not achieved general acceptance for use in offshore units, the reason being that as regulations regarding toxicity and biodegradability of chemicals that could potentially be spilled into the ocean have become more severe, the potential number of acceptable absorbents has become correspondingly more limited. Acid gas clean-up on off-shore platforms has therefore come to require absorbents to be selected for with lower toxicity and higher biodegradability.

Summary of the Invention

[0007] We have now identified a class of absorbents which have high selectivity for the removal of H₂S in the presence of CO₂ with very acceptable environmental properties permitting their use in offshore installations such as natural gas production platforms.

According to the present invention, therefore, we provide a process for the selective absorption of normally gaseous acid components from gas mixtures containing both the acidic component and gaseous non-acidic components, which process is carried out in a gas separation unit located at an offshore marine installation. The preferred asorbents used in the process comprise severely sterically hindered amino ethers, including ether alcohols, bis-(amino) ethers and alkoxy amino ethers; mixtures of the amino ether compounds may be used. The process is capable of selectively removing H₂S from gas mixtures which also contain CO₂ and so makes it useful for treating natural gas from fields containing both these acidic components.

[0008] The invention also provides a gas separation unit containing a liquid absorbent comprising hindered amino ethers and ether alcohols. Offshore petroleum fluids production installations having a gas separation unit with one of these sorbents are also provided. The separation unit includes a cyclic amine absorption natural gas purification unit for separating acidic gases from produced petroleum gas; this unit has an absorption tower and a regeneration tower through which an aqueous amine absorbent solution is circulated to absorb acidic gases from the gas in the absorption tower and to desorb acidic gases in the regeneration tower. The purified petroleum gas and at least one stream of acidic gas removed from the gas are recovered as separate streams from the regenerator.

Drawings

[0009] The single Figure of the accompanying drawings is a graph showing the

biodegradability of several candidate compounds as reported below.

Detailed Description

General Processing Features

[0010] The acid gas sorbents used in the present gas separation process are normally used in the form of aqueous solutions which can be circulated in the normal type of continuous cyclic amine gas purification unit mentioned briefly above, comprising essentially an absorber tower in which the aqueous amine solution is contacted in countercurrent flow with the incoming gas mixture. The liquid amine stream is then passed to a regenerator in which the sorbed gases are desorbed by a change in conditions, typically a reduction of pressure or an increase in temperature in a separate tower although stripping with another gas stream may also be utilized; the regenerated sorbent solution and the desorbed gases leave the regenerator tower as separate streams. The present amine sorbents can be used in the same manner as conventional amine sorbents and consequently, similar operating practices in the units containing these sorbents can be followed.

[0011] The processed gas mixtures include H₂S, and may optionally include other acidic gases such as CO₂, SO₂, COS, HCN, as well as non-acidic gases such as N₂, CH₄, H₂, CO, H₂O, C₂H₄, NH₃, and the like. High selectivity for H₂S absorption is favored for the present purposes although less selective absorption is not excluded when required by the feed gas or purification needs. If processing conditions are adjusted non-selective removal of the acid gas components from the non-acidic components may be achieved with subsequent separation of the acidic gases one from another, e.g., separation of H₂S from CO₂, allowing the CO₂ to be re-injected for reservoir pressure maintenance.

[0012] The preferred absorbents used in the separation units are the severely sterically hindered amino ethers, ether alcohols and alkoxy amino ethers, with especial preference given to the amino ether derivatives of triethylene glycol.

[0013] The hindered amine ethers are used in the form of aqueous solutions, typically from about 0.1 to 5M concentration in order to secure adequate loading; variations both within this range and outside it may be made according to individual processing requirements, e.g., concentration of gas species in total gas flow, size of unit, etc. In most cases, the rich solution will have an amine concentration of 0.05 to 2.5 M. Conditions in the separation unit will be typical of those used in conventional amine gas purification processes, for example, in temperature swing operation, sorption temperatures are typically in the range of 30-50°C, more usually 40-50°C and desorption temperatures typically at 60 to 140°C, e.g., 100- 125°C. In pressure swing operation the sorption and desorption pressures are usually set by the pressure of the incoming feed stream and perhaps also by any requirement for the product stream.

[0014] A typical procedure for the selective H₂S removal phase of the process comprises selectively absorbing H₂S in countercurrent contact of the gaseous mixture is described in US 2009/00308248 to which reference is made for this description.

Production Installations

[0015] The gas purification or separation unit is situated in a marine, offshore location, typically on an offshore gas or crude oil production platform. In the case of a platform producing from an oilfield, the gas will be the natural hydrocarbon gases which are co- produced with the crude oil and which are separated from the oil on the platform to stabilize the liquid before transport either by pipeline or by offloading onto a transfer vessel.

Production platforms may be fixed to the ocean floor as with the familiar and conventional rigid (concrete or steel) leg platforms or the concrete gravity base structures such as the Condeep platforms used in locations usually no more than 200 m in depth although some Condeep structures have been installed in about 350 m of water. Fixed platforms of this type have usually provided adequate space for processing equipment. In deeper water, for example, over 500 m depth, fixed platforms are not economically feasible and floating production, storage and offloading structures tethered to the seabed in a manner that eliminates most vertical movement of the structure, such as tension leg platforms, SPAR or Deep Draft Caisson Vessels (DDCVs), are used at greater depths up to about 2,000 m with one currently placed in over 2400 m (Perdido SPAR in the Gulf of Mexico in 2,438 meters of water). The gas processing unit and related equipment will be installed on the structure of whatever kind in a manner conformable to space and stability requirements. The produced gases may be handled according to the location with close offshore platforms discharging the purified natural gas into the pipeline to shore and, when pipelining to shore is not an option as in the deepwater locations, to the related storage facilities either on the same platform or on another nearby storage facility. CO₂ is frequently re-injected into the formation to improve recovery of the oil or gas and for this purpose, the CO₂ will be sent to the re-injection compressor equipment. Separated H₂ may be handled in the same way or, if possible, treated in a Claus plant and the product sulfur stored for later disposal. On far offshore installations not linked to shore by pipeline, gas liquefaction facilities can be provided to store the hydrocarbon gases as well as separated gases pending transfer to a vessel for transport ashore.

Absorbents

[0016] One class of H₂S selective absorbents which are predicted to exhibit favorable environmental characteristics, particularly aquatic toxicity, are the hindered amine alkylsulfonate and alkylphosphonate salts which are described in US 2009/0308248, to which reference is made for a description of these salts as well as of their synthesis and use in selective gas separation processes. Briefly, the salts are generally represented by the following formulae:

in which R¹, R², R³ and R⁴ are the same or different and selected from H, C1-C₉ substituted or unsubstituted straight or C₃-C₉ substituted or unsubstituted branched chain alkyl, C₃-C₉ cycloalkyl, C₆-C₉ aryl, alkylaryl, arylalkyl, C₂-C₉ straight or branched hydroxyalkyl, cycloalkyl and mixtures thereof provided that both R¹ and R² are not hydrogen and, when n is 2 or more, R³ and R⁴ on adjacent carbon or on carbons separated by one or more carbons, can be a cycloalkyl or aryl ring and, when the substituents are substituted, they are heteroatom containing substituents, preferably an -NR⁵R⁶ group wherein R⁵ and R⁶ are the same or different and are selected from H, C1-C9 straight or C3-C9 branched chain alkyl, C3-C9 cycloalkyl, C₆-C₉ aryl, alkylaryl, arylalkyl, C₂-C₉ straight or branched chain hydroxyalkyl, cycloalkyl, provided that R⁵ and R⁶ are not both H, and further, when R¹ is H, and n is 2 or more, R² and R³ or R⁴ on the carbon at least one carbon removed from the aminic nitrogen can form a ring;

n is an integer of 1 or more, preferably 1 to 4, more preferably 2 to 4;

metal cation is one or more monovalent, divalent or trivalent metal cation(s) sufficient to satisfy the valence requirements of the anion(s), for example, magnesium, barium, sodium, lithium, potassium or calcium with preference for sodium and potassium. Salts formed from divalent cations can be half- or full-salts.

[0017] R¹ and R² (R¹ and R² are not both hydrogen) are preferably selected from H, C₄-C₆ alkyl, more preferably C₄-C₆ branched chain alkyl, most preferably tertiary-butyl. R³and R⁴ are normally H or C₂-C₃ alkyl. The value of n is preferably from 1 to 4, most preferably 2 or 3.

[0018] For optimal sorption of the acidic component(s) of the gas mixture, it is necessary to use the salts, preferably the alkali metal salts in order to maintain a reserve of alkalinity in the sorbent solution: the free acids are relatively less effective.

[0019] The sulfonate and phosphonate salts may be synthesized by the methods described in US 2009/0308248 to which reference is made for a description of such methods.

[0020] The preferred absorbent materials for offshore use are the severely sterically hindered amino ethers and amino alcohols of polyalkyleneglycols, especially diethylene glycol and, more preferably triethylene glycol. These have been shown to be selective for absorption of H₂S in the presence of C0₂ and other acidic gases in mixtures with non-acidic gases. The hindered amino derivatives of triethylene glycol have been found to be particularly favorable from the environmental point of view. These absorbents have been found to exhibit high selectivity for H₂S absorption in the presence of acidic gases such a C0₂ and from non-acidic gases. [0021] The preferred amino ethers for offshore application are defined by the formula:

where R¹ is a secondary or tertiary alkyl group of 3 to 8 carbon atoms, preferably a tertiary group of 4 to 8 carbon atoms, Y is H or alkyl of 1 to 6 carbon atoms, n is a positive integer from 3 to 8 and x is a positive integer from 3 to 6. The preferred R¹ group is tertiary butyl and the most preferred amino ethers are those derived from triethylene glycol (n is 2, x is 3). When Y is H, the amino ether is an amino ether alcohol such as tert-butylamino ethoxyethoxyethanol, derived from triethylene glycol; when Y is alkyl, preferably methyl, the amino ether is an alkoxy amino ether, with preference for tert-butylamino methoxy- ethoxyethoxyethanol. The monoamino ethers may be used in blends with diamino ethers in which the terminal OH group of the ether alcohol or the terminal alkoxy group of the alkoxy amino ether is replaced by a further hindered amino group as expressed in the formula:

where R¹, n and x are as defined above and R², which may the same or different to R¹, is a secondary or tertiary alkyl group of 3 to 8 carbon atoms. A preferred diamino ether of this type is bis-(t-butylamino ethoxy) ethane which may conveniently be used as a mixture of ferf-butylamino methoxy-ethoxyethoxyethanol and bis-(t-butylamino ethoxy) ethane.

[0022] Preferred examples of these amino ethers are disclosed in U.S. Patents Nos.

4,405,583; 4,405,585, 4,471 , 138, 4,894, 178 and U.S. Patent Publication 2010/0037775, to which reference is made for a full description of these materials, their synthesis and their use in selective acidic gas separation processes. Their disclosures are summarized below for convenience.

[0023] US 4,405,583: The hindered diamino ethers disclosed in this patent are defined by the formula:

where R¹ and R⁸ are each Ci to C₈ alkyi and C₂ to C₈ hydroxyalkyi groups, R², R³, R⁴, R⁵,R⁶, and R⁷ are each hydrogen, C1-C4 alkyi and hydroxyalkyi groups, with certain provisos to define the adequately hindered molecule and m, n, and p are integers from 2 to 4 and o is zero or an integer from 1 to 10. A typical diamino ether of this type is 1 ,2-bis(ferf- butylaminoethoxy) ethane, a diamino derivative of triethylene glycol.

[0024] US 4,405,585: The hindered amino ether alcohols disclosed in this patent are defined by the formula:

where R¹ is CrC₈ primary alkyi and primary C₂-C₈ hydroxyalkyi, C₃-C₈ branched chain alkyi and branched chain hydroxyalkyi and C₃-C₈ cycloalkyl and hydroxycycloalkyl, R², R³, R⁴ and R⁵ are each hydrogen, C1-C4 alkyi and C1-C4 hydroxyalkyi radicals, with the proviso that when R¹ is a primary alkyi or hydroxyalkyi radical, both R² and R³ bonded to the carbon atom directly bonded to the nitrogen atom are alkyi or hydroxyalkyi radicals and that when the carbon atom of R¹ directly bonded to the nitrogen atom is secondary at least one of R² or R³ bonded to the carbon atom directly bonded to the nitrogen atom is an alkyi or hydroxyalkyi radical, x and y are each positive integers from 2 to 4 and z is an integer from 1 to 4. Exemplary compounds of this type include the amino ether alcohol tert- butylaminoethoxyethanol, a derivative of diethylene glycol.

[0025] US 4,471 , 138: This patent discloses the desirability of using a combination of a diamino ether with an aminoether alcohol. The two compounds are represented by the respective formulae:

where x is an integer ranging from 2 to 6. This mixture can be prepared in the novel one- step synthesis, by the catalytic tertiary butylamination of a polyalkenyl ether glycol, HO-(CH₂CH₂O)_x-CH₂CH₂-OH, or halo alkoxyalkanol. For example, a mixture of bis-(ferf- butylaminoethoxy)ethane (BTEE) and ethoxyethoxyethanol-ferf-butylamine (EEETB) can be obtained by the catalytic fert/ary-butylamination of triethylene glycol. The severely hindered amine mixture, e.g., BTEE/EEETB, in aqueous solution can be used for the selective removal of H₂S in the presence of C0₂ and for the removal of H₂S from gaseous streams in which H₂S is the only acidic component, as is often the case in refineries.

[0026] US 4,894, 178: A specific combination of diamino ether and aminoalcohol represented by the respective formulae:

with x being an integer ranging from 2 to 6 and the weight ratio of the first amine to the second amine ranging from 0.43:1 to 2.3:1 . This mixture can be prepared in the one-step synthesis, by the catalytic tertiary-butylamination of the corresponding polyalkenyl ether glycol, for example, by the catalytic tertiary-butylamination of triethylene glycol. This mixture is one of the preferred absorbents for use in offshore gas processing.

[0027] US 2010/0037775: The reaction of a polyalkenyl ether glycol with a hindered amine such as ferf-butylamine is improved by the use of an alkoxy-capped glycol. In the case of alkoxy DEG, the capped glycol now precludes the formation of an unwanted cyclic byproduct, ferf-butyl morpholine (TBM). A preferred capped glycol is methoxy-triethylene glycol although the ethoxy-, propoxy- and butoxy homologs may also be used. The reaction between monomethoxy triethylene glycol and ferf-butylamine is shown to produce MEEETB almost exclusively, in -95% yield, eliminating the need for extensive distillation to remove the product.

[0028] The amino ether compounds may be used in conjunction with other related materials such as an amine salt as described in U.S. Patent No. 4,618,481 . The severely sterically hindered amino compound can be a secondary amino ether alcohol or a disecondary amino ether. The amine salt can be the reaction product of the severely sterically hindered amino compound, a tertiary amino compound such as a tertiary alkanolamine or a triethanolamine, with a strong acid, or a thermally decomposable salt of a strong acid, i.e., ammonium salt or a component capable of forming a strong acid.

[0029] Similarly, U.S. Pat. No. 4,892,674 discloses a process for the selective removal of H₂S from gaseous streams using an absorbent composition comprising a non-hindered amine and an additive of a severely-hindered amine salt and/or a severely-hindered aminoacid. The amine salt is the reaction product of an alkaline severely hindered amino compound and a strong acid or a thermally decomposable salt of a strong acid, i.e., ammonium salt.

Selectivity of Candidate Compounds

[0030] Three characteristics which are important in determining the effectiveness of the amino compounds herein for H₂S removal are "selectivity", "loading" and "capacity".

"Selectivity" is defined as the mole ratio fraction of the H₂S to the CO₂ in the liquid (sorbent solution) phase to the mole ratio fraction of the H₂S to the CO₂ in the gaseous phase. The higher this fraction, the greater the selectivity of the absorbent solution for the H₂S in the gas mixture. "Loading" is the concentration of the H₂S and CO₂ gases physically dissolved and chemically combined in the absorbent solution expressed in moles of gas per moles of the amine. The amino compounds used in the present invention typically have a "selectivity" of not substantially less than 10 at a "loading" of 0.1 moles, preferably, a "selectivity" of not substantially less than 10 at a loading of 0.2 or more moles of H₂S and CO₂ per moles of the amino compound. "Capacity" is defined as the moles of H₂S loaded in the absorbent solution at the end of the absorption step minus the moles of H₂S loaded in the absorbent solution at the end of the desorption step. High capacity enables one to reduce the amount of amine solution to be circulated and use less heat or steam during regeneration.

Selectivity = (H2S/CO2) in solution/(H2S/CO2) in feed gas

Loading = Moles H2S/Moles absorbent compound

Capacity = Moles H2S absorbed / Moles H2S after desorption

Moles H2S absorbed The selectivity of the preferred amino glycol derivatives is demonstrated by comparison of the following absorbents:

EETB Ethoxyethanol-tert-butylamine (tert-butylamino-ethoxy-ethanol)

MEETB Methoxyethoxyethanol-tert-butylamine

EEETB Ethoxyethoxyethanol-tert-butylamine

BEETB Butoxyethoxyethanol-tert-butylamine

MEEETB Methoxyethoxyethoxyethanol-tert-butylamine

TEGTB Triethylene glycol-t-butylamine (t-butylaminoethoxyethoxyethanol)

Bis-SE Bis-(t-butylaminoethyl) ether

Bis-TEGTB Bis-(t-butylamino ethoxy) ethane (bis-(t-butylamino) triethylene glycol)

[0031] Experimental Procedure

1. Absorption tests were carried out at 35° C. on 0.15 M aqueous solutions of absorbent using a gas mixture of nitrogen:carbon dioxide:hydrogen sulfide of 89:10:1 for 2 hours.

2. Desorption experiments were run at 85° C. in flowing nitrogen for 2 hours at the same flow rate as the test gas mixture.

[0032] The results are shown in Table 1 below.

[0033] As can be seen, the methoxy-, ethoxy- and butoxy-substituted diethylene and triethylene glycol-t-butyl amines have higher degrees of selectivity as compared to the EETB and its diamino derivative (Bis-SE, bis-(t-butylaminoethyl) ether) and have at least equivalent and in most cases superior capacity and superior selectivity after regeneration than the EETB and the corresponding diamino bis-SE.

Assessment of Health and Environmental Aspects of Candidate Compounds

[0034] To assess the toxicity potential and environmental fate properties of various selective absorbents, quantitative structure activity relationships (QSARs) were applied together with experimental confirmation of aquatic toxicity.

[0035] The chemical structures of candidate absorbents were run through a series of computer models for comparative purposes. Physical chemical properties (i.e., vapor pressure, water solubility, and octanol/water partition coefficient) were estimated using two models, EPISuite¹ and SPARC². Biodegradation potential was determined using BlOWin, a subroutine of EPISuite.

[0036] The four candidates in the evaluation were:

Candidate A EETB

Candidate B MEEETB

Candidate C TEGTB

Candidate D Bis-TEGTB

Biodegradation

[0037] Table 2 below compares physical chemical properties (VP, WS, Log K_ow) of the candidate substances. The octanol/water partition coefficient (or Log K_ow) of all candidate substances indicates these substances would not be expected to pose a bioaccumulation concern.

[0039] The biodegradation of the four candidates was tested by Manometric Respirometry following OECD TG 301 F [at 20°C] with the results in Table 3 below and in the

accompanying Figure.

[0040] The continued upward trend in the biodegradation of the mixture of C and D indicates that degradative elimination from the environment can be expected with increasing time.

Aquatic Toxicity

[0041] Aquatic toxicity predictions for fish, invertebrates (Daphnia) and algae were made using ECOSAR, also a subroutine of EPISuite that estimates aquatic toxicity and verified experimentally. The commercial TOPKAT® ⁴model was used to estimate mammalian toxicity endpoints.

[0042] The acute aquatic toxicity predictions in Table 4 indicate absorbents A, B, E and F exhibit toxicity to at least one aquatic organism in the 10-100 mg/l range . Fish appear to be consistently less sensitive than daphnids or algae.

[0043] Aquatic toxicity was tested experimentally using the OECD TG 202 - Daphnia sp. Acute Immobilisation Test The results are given below in Table 5.

Table 5

Aquatic Toxicity

⁴ Accelrys Discovery Studio Predictive Toxicology tool, Discovery Studio TOPKAT.

[0044] The classification "Harmful to aquatic organisms" signifies that the compounds in question may be used in the offshore environment subject to mitigation, for example, secondary treatment or dilution. None were deemed toxic, barring their use. Based on biodegradability and aquatic toxicity predictions none of the candidate substances are expected to require a negative environmental label (e.g., the European dead fish/dead tree symbol) although absorbent D appeared on the basis of the predictions to be least preferred from an environmental perspective.

Mammalian Toxicity

The TOPKAT® predictions for mammalian toxicity endpoints given in Table 6 indicate absorbents A, and C have a low potential for acute toxicity in rats, while absorbents B and D show predicted acute toxicity in the range of 1000 to 2000 mg/kg, which would put them in the harmful category. Chronic toxicity in rats is reported as the Lowest Observed Adverse Effect Level (LOAEL), which is the lowest dose level, in weight of chemical to body weight units, which is predicted to cause an adverse effect. The Ocular Irritancy module computes the probability of a chemical structure being an ocular irritant in the Draize test. All candidates are expected to cause severe eye irritation. The Developmental Toxicity Potential module of the TOPKAT package predicts that candidate A derived from diethylene glycol is likely to be less favorable than the triethylene glycol derivatives.

[0045] Carcinogenic potential is predicted using the NTP Rodent Carcinogenicity Module in TOPKAT and comprises four statistically significant quantitative structure-toxicity relationship models. These models are derived from 366 uniform rodent carcinogenicity studies conducted by the National Cancer Institute. Positive results listed in Table 4 below indicate the potential for the candidate to be carcinogenic or not carcinogenic in either rats or mice. Results scored as indeterminate indicate insufficient evidence to score either as positive or negative. The model also predicts that none of the candidate absorbents are expected to be skin sensitizers, nor are they expected to be mutagens.

Claims

1. A marine offshore petroleum fluid production installation including a cyclic amine absorption natural gas purification unit for separating acidic gases from produced petroleum gas, the unit comprising an absorption tower and a regeneration tower through which an aqueous amine absorbent solution is circulated to absorb acidic gases from the gas in the absorption tower and to desorb acidic gases in the regeneration tower to produce a stream of purified gas and at least one stream of acidic gas removed from the gas, the aqueous amine absorbent solution comprises an aqueous solution of a severely sterically hindered amino ether of the formula:

where R¹ is a secondary or tertiary alkyi group of 3 to 8 carbon atoms, Y is H or alkyl of 1 to 6 carbon atoms, n is a positive integer from 3 to 8 and x is a positive integer from 3 to 6.

2. A marine offshore petroleum fluid production installation according to claim 1 in which R¹ is a branched secondary or tertiary alkyi group of 3 to 9 carbon atoms.

3. A marine offshore petroleum fluid production installation according to claim 2 in which R¹ is tertiary butyl.

4. A marine offshore petroleum fluid production installation according to claim 3 in which n is 2.

5. A marine offshore petroleum fluid production installation according to claim 1 in which x is 3.

6. A marine offshore petroleum fluid production installation according to claim 1 in which Y is H

7. A marine offshore petroleum fluid production installation according to claim 6 in which the amino ether is tert-butylamino ethoxyethoxyethanol.

8. A marine offshore petroleum fluid production installation according to claim 1 in which Y is methyl.

9. A marine offshore petroleum fluid production installation according to claim 1 in which the amino ether is ferf-butylamino methoxy-ethoxyethoxyethanol.

10. A marine offshore petroleum fluid production installation according to claim 1 in which the absorbent solution also comprises a diamino ether of the formula:

where R¹, n and x are as defined in claim 1 and R², which may the same or different to R¹, is a secondary or tertiary alkyl group of 3 to 8 carbon atoms.

1 1 . A marine offshore petroleum fluid production installation according to claim 1 in which the absorbent solution also comprises bis-(t-butylamino ethoxy) ethane..

12. A marine offshore petroleum fluid production installation according to claim 1 1 in which the absorbent solution comprises ferf-butylamino methoxy-ethoxyethoxyethanol and bis-(f-butylamino ethoxy) ethane.

13. A process for the selective absorption of normally gaseous acidic components from hydrocarbon gas mixtures containing both the acidic component and gaseous non-acidic components, which process is carried out in a gas separation unit located at an offshore marine petroleum fluid production installation in which an aqueous amine absorbent solution is circulated in a cyclic amine absorption natural gas purification unit to absorb acidic gases from the hydrocarbon gas in an absorption tower and to desorb acidic gases in a regeneration tower to produce a stream of purified hydrocarbon gas and at least one stream of acidic gas removed from the hydrocarbon gas, the aqueous amine absorbent solution being an aqueous solution of a severely sterically hindered amino ether of the formula:

where R¹, Y, n and x are as defined in anyone of the preceding claims.

14. A process according to claim 13 in which H₂S is selectively removed from a produced natural gas stream which contains H₂S and CO_2.

15. A process for purifying a stream of natural gas produced at a marine offshore petroleum fluid production installation including a cyclic amine absorption natural gas purification unit for separating acidic gases from produced natural gas, the unit comprising an absorption tower and a regeneration tower through which an aqueous amine absorbent solution is circulated to absorb acidic gases from the natural gas in the absorption tower and to desorb acidic gases in the regeneration tower to produce a stream of purified gas and at least one stream of acidic gas removed from the natural gas, the aqueous amine absorbent solution being an aqueous solution of a hindered, wherein the absorbent solution also comprises a diamino ether of the formula:

where R¹, Y, n and x are as defined in claim 1 and R² is as defined in anyone of claims 1 - 12.

16. A process according to claim 15 which selectively absorbs H₂S from the natural gas.