METHOD OF DECONTAMINATING EARTH AND/OR NATURAL GAS PROCESSING EQUIPMENT

Abstract: Surface layers of the earth contaminated with precipitates of alkaline earth metal sulfates including radium sulfate derived from subterranean waters brought to the surface of the earth, are decontaminated using an aqueous chemical composition including a polyaminopolycarboxylic acid such as ETDA or DTPA in combination with a synergist, preferably oxalate or monocarboxylic acid anion such as salicylate. The surface layers may be decontaminated in situ by applying the solvent to the earth to bring the precipitates into dissolved form after which the dissolved precipitates are leached into lower layers of the earth by percolation with water. Alternatively, the earth may be removed from its original site and decontaminated in a tank or lined pond after which the decontaminated earth may be returned to its approximate original site. There is also disclosed a method of decontaminating natural gas processing equipment using the aqueous chemical composition.

Description: METHOD OF DECONTAITO-ATTNG EARTH AND/OR NATURAL GAS PROCESSING EOUIFMEKT ϊhis invention relates to a method of decontai rating earth and/or natural gas processing equipment. Natural gas is a major and attractive energy source in the United States and other countries which is distributed on a wide scale by means of pipelines to the __ltiιnat_. users. The cαπposi iαn of natural gas at the wellhead varies widely from field to field and many cαrponents may need to be removed by processing before delivery to the pipeline, as noted in Encyclcpedia of Chemical Technology, _ixk-Oth_ver, Third Edition, Vol. 1, pp. 630-652, John Wiley & Sons, New York, 1978. Condensate must be removed frcm wet gas, both to eliminate the possibility of condensation in the pipeline itself and to separate these cαrπponents as another marketable product. Water vapor must also be removed to preclude the formation of gas hydrate and hydrogen sulfide is removed because of its poisonous and corrosive characteristics. Other cxxπponents such as carbon dioxide and helium may also require removal if they are present. A number of different processing techniques have been developed for the removal of specific contaminants in the gas and depending upon the composition of the wellhead gas, one or more of the specific processing techniques may be employed at any given gas production site. Water, for example, is generally removed either by absorption in a hydroscopic liquid or adsorption on an activated solid dessicant. Acid gases such as carbon dioxide, hydrogen sulfide and other sulfur ccarpσunds may be removed by processes such as the Sulfinol and Selexol processes or by alkali scrubbing, normally using an organic sc tibbing agent such as ικDnoet_hanolamine, diethanolamine or triethanolamine. Natural gas liquids may be recovered by oil absorption or, more recently, by the cryogenic turboexpander process. Regardless of the specific processing sequence used to condition the gas for pipeZLining, it is normally passed through a number of items of process equipement prior to removal of the water which generally is present in all wellhead gas. Conventionally, the gas will pass through filters to remove entrained solid ∞ntaminants as well as cαπpressαrs and other items of process equipment employed in the purification train. One problem which is encountered with these items of equipment which precede the water removal is that mineral species and other contaminants from the producing formations may be dissolved in or entrained with the water and may contaminate the equipment with which it comes into contact. Among the cxsntaminants of this kind are dissolved salts including, especially, mineral species of low solubility which may deposit as scale on the filters and other surface equipment. Among the minerals of this kind which cause a particular problem are the εulfates of the alkaline earth metals, including, in particular, calcium, strontium and barium. Many subterranean waters contain alkaline earth metal cations, such as barium, stxαntium, calcium and magnesium, and anions, such as sulfate, bicarbonate, carbonate, phosphate, and fluoride. When ccatibinations of these anions and cations are present in cxra_sntratiσns viiich exceed the solubility product of the various species which may be formed, precipitates form until the respective solubility products are no longer exceeded. For example, when the concsatrations of the barium and sulfate ions exceed the solubility product of barium sulfate, a solid phase of barium sulfate will farm as a precipitate. Solubility products are exceeded for various reasons, such as evaporation of the water phase, change in pH, pressure or tempera ure and the .Introduction of additional ions which can form insoluble ∞πpσunds with the ions already present in the solution. As these reaction products or mineral species precipitate on the surfaces of the water-carrying or water-conta__ning system, they form adherent deposits or scale. Scale may prevent effective heat transfer, interfere with fluid flew, facilitate corrosive processes, or harbor bacteria. Scale is an expensive problem in many industrial water systems, in production systems for oil and gas, in pulp and paper mill systems, and in other systems, causing delays and shutdowns for cleaning and removal. The scale deposits frcm the sulfates of the alkaline earth metals, including barium and strontium sulfate scale deposits present a unique and particularly intractable problem. Under most conditions, these sulfates are considerably less soluble in all solvents than any of the other ccmmonly encountered scale-foraing compounds, as shown by the ccaiparative solubilities given in Table 1 belcw. Table 1 Comparative Solubilities- 25°C in Water. Scale Solubility, ./I. Gypsum 2080.0 Strontium sulfate 140.0 Calcium Carbonate 14.0 Barium sulfate 2.3 It is generally acknowledged that barium sulfate scale is extremely difficult to remove chemically, especially within reasonably short periods of time: the solvents which have been found to work generally take a long time to reach an equilibrium concentration of dissolved barium sulfate, which itself is usually of a relatively low order. Consequently, barium sulfate must be removed mechanically or the equipment, e.g.pipes, etc. , containing the deposit must be discarded. Another problem associated with the formation of barium and st__ tlum sulfate scales is that radium, another member of the alkaline earth group of metals, tends to be deposited at the same time in the farm of an insoluble sulfate so that the equipment becomes radioactive, and may eventually beccsme unusable far safety reasons alone. At present a considerable amount of oilfield tubular goods are in this condition and cannot be readily restrαred to usable condition because of the difficulty of __emσving the radioactive scale. The principal isotopes of radium which have been identified in these scale deposits are radium-226 and radium-228, with half-lives of 1600 years .an about 5.8 years, respectively, so that there is a considerable potential hazard if they are allowed to remain on the equipment. Radioisotcpes of metals such as thallium and thorium e.g. thallium-208, __hαrium-232 and other radioactive isotopes - frequently farmed by the decay of uranium - may also be deposited with the radium with the same result. This problem is encountered with gas processing equipment where the filters and dehydration media, including screens, sσrbent beds and media e.g. silica, charcoal or alumina may become quite radioactive with extended use. Since these radioactive elements are embedded in the scale which itself can be removed only with difficulty, the decontamination of the equipment and material is a substantial problem. Ωie incidence of barium sulfate scale is worldwide, and it occurs principally in systems handling subsurface waters. Because of this, the barium sulfate scale problem is of particular concern to the petroleum industry as water is «_ generally produced with petroleum and as time goes on, more petroleum is produced by the waterflooding method of secondary recovery, iπplying even greater volumes of produced water. The scale may occur in many different places, including production tubing, well bore perforations, the area near the well bare. gathering lines, meters, valves and in other production equipment. Barium sulfate scale may also form within subterranean formations such as in disposal wells. Scales and deposits can be formed to such an extent that the permeability of the formation is irrpaired resulting in lower flow rates, higher pump pressures, and ultimately abandonment of the well. Barium sulfate scale is particularly troublesome when sulphate-rich seawater is used as an injection fluid in oil wells whose formation water is rich in barium ions. This particular aspect of the barium scale problem is severe in some U.S. oil fields as well as some older North Sea oil fields. Scaling of this nature is also expected to occur during advanced production stages in other North Sea fields particularly after seawater breakthrough has taken place. As noted in our copending patent application of even date entitled "Sulphate Scale Dissolution", various proposals have been made in the past for the removal of barium sulfate scales using chemical scale removal compositions. Examples of such scale removal techniques are to be found in US-A-2,877,848; US-A-3,660,287; US-A-4,708,805; US-A-4,190,462; US-A-4,215,000 and US-A-4,288,333. The proposals set out in these dislosures represent, however, only partial or unsatisfactory solutions to the scale removal problem. Our copending Patent application referred to above dissolution, discloses highly effective chemical scale removal cσrrpositions which may be used for removing alkaline earth sulfate scales from oil field equipment including tubular goods such as pipe, casing, and wellhead equipment such as meters, valves and above-groiind piping. Reference is made to this copending application for disclosure of these scale removal compositions and the methods by which they may be used. Although a principal problem area is with the deposition of these scale materials on oilfield equipment, there is a related problem which is that the earth around the equipment may become c_αntaminated with these scale materials together with any associated radioactive components, if the subsurface waters are allcwed to spill out onto the surface of the earth during normal operations. This may occur, for example, if subsurface waters are brought to the surface during drilling or production and stored in ponds from which they can seep into the surrounding earth layers. Another source of cx.ntaiirina.tion of this kind is when attempts are made to remove scale from equipment by the use of various chemical scale removal solvents which are allowed to spill onto the surface of the earth and then to seep into it. In either case, the alkaline earth metal sulfates and any other potential scale-forming materials enter the earth layers near the surface and form insoluble precipitates in these layers of the earth. Because these precipitates may also contain radium, the earth formations into which the subterranean waters enter may be subject to cαntamination with these radioactive scale deposits when, as is usually the case, the ∞nditions are appropriate for precipitation of the scale. In particular, if the subterranean waters are permitted to flood onto the surface of the earth, the surface earth and closely adjacent levels of the earth may become coni_aminated with the radioactive deposit and after a period of time may became undesirably radioactive, with a relatively high level of background radiation. Clearly, it is desirable to return surface formations of the earth to a condition where background radiation is reduced to a low level and also to remove insoluble materials such as alkaline earth metal scales which may have been deposited by invasion of top surface waters. The present invention provides an effective means for this to be done. According one aspect of the present invention, deposits of water insoluble alkaline earth metal sulfates, which may include radioactive cc∑nta inants such as radium sulfate, are removed from the earth by the use of a chemical cxmposition which includes a chelant (chelating agent) in cxatibination with a catalyst or synergist which increases the solubility of the alkaline earth metal sulfates in aqueous solution. The preferred catalyst or synergist is the oxalate aniαn, but other synergists may also be used including the monocarboxylate anion, the thiosulfate anion, or the nitriloacetic acid aniαn, as described in our copending application referred to above. The earth around the oil field production equipment including wellheads, mud ponds, tubing stacks or any other place exposed to scaled equipment or the invasion of produced subsurface waters may be deconi^aminated ty leaching the naturally occuring radioactive material (NORM) and scale frcm the earth and permitting the leachate to percolate into a secure, subterranean layer of the earth. Alternatively, the soil may be removed from around the equipment and the scale and NORM leached out in a tank. Ηie leached soil can then be returned approximately to its former location, thereby avoiding the expense of removing the offending surface soil to a hazardous waste disposal site with the resultant transport and disposal expenses. In this case, the leachate may be recovered and treated fcy normal chemical methods if the radioactive material is wanted or, if not, the leachate may be returned to the subterranean formation from which the alkaline earth metal scale and NORM were derived. In this way, the contamina ing material is returned to its original situs deep in the earth where it presents no danger. A second aspect of the invention relates to a method for the decontamination of gas handling equipment and media such as pipes, tubing, pumps, sαrption media and vessels, which is effective and convenient for the removal of radioactive scales and deposited mineral species. According to the second aspect of the present invention, deposits of insoluble, radioactive sulfate scale are removed from natural gas processing equipment by the use of a chemical composition which includes a chelant (chelating agent) in ccmbination with a catalyst or synergist which increases the solubility of the alkaline earth metal sulfates in aqueous solution. The preferred catalyst or synergist is the αxalate anion, but other synergists may also be used .including the monocarbc__ylic acid anion, the thiosulfate anion or the nitriloacetic acid anion disclosed in one expending patent application referred to above. In both aspects of the invention the chelant may, for example, be selected from aii nocarboxylic acids, polyaminocarboxylic acids, polyandries, salts and mixtures thereof. Ihe synergist may be selected from anions or organic or inorganic acids, and mixtures thereof, having an iαnizatiαn -2 -2 constant of less than substantially 10 (Ka <10 ) . Reference is now made to the acccmcpanying drawings which shows in simplified form, a section of the earth with oil field production equipment in place through various subterranean formations. The surface earth formations *_ich may be treated acx_ording to the first aspect of the present invention are usually those areas of the earth's surface and in the immediately adjacent subsurface layers which surround boreholes extending frαn the surface of the earth into subterranean formations where subsurface waters containing alkaline earth cations are found. Generally, boreholes of this type are used for the production of petroleum, natural gas and other minerals e.g. sulfur. During the driLlling, completion or production phases of the life of the well, greater or lesser quantities of these subsurface waters may be brought to the surface of the earth where they will contaminate the equipment and the surface layers of the earth if they are not rigorously contained. Since the level of xsntamination is usually fairly small, rigorous containment has often not been applied in the past, but constant invasion of the surface layers by such waters may, over extended periods of time, result in an undesirable accπimulation of NORM as well as the less harmful materials with similar chemistry. Accumulation of the NORM and scale may also occur around field equipment including tubing stacks or anywhere that scale equipment has been handled, particularly where scale has been removed using either known scale removal cαrpositions or the highly effective scale removal cσπpositions disclosed in the copending application referred to above. Ac__ording to the first aspect of the present invention, the scale and NORM deposits are removed from the surface earth layers by leaching with a scale removal composition. The removal process may be carried out with the surface earth layer remaining tindisturbed at its original situs or, alternatively, by removal of the earth to a tank or pond (with an iπpervious liner such as clay or plastic sheeting) in which the contaminants are removed using the aqueous composition. After the scale and NORM have been leached out from the earth, the decontaminated earth is brought back more or less to its original site and replaced. Methods for decontamination of surface earth layers in this manner are cσirparable to those which have been used for the removal of uranium fran surface earth formations in areas of the Southwestern United States, including Texas and New Mexico. If the contaminants are leached from the earth while it remains at its original situs, the character of the subsurface layers and formations should be ascertained in order to ensure that the leaching solution together with the leached-σut contaminants does not enter any subsurface aquifers or other formations which should be maintained in a pristine condition. Thus, aquifers should be protected by an overlying irrpervious layer e.g. of clay or another iπpervious stratum. If this option is not, however, available, it may be necessary to resort to the earth removal technique referred to above, with the leachate solution (xaitaining the radioactive contaminants being treated separately to remove the contaminants e.g. by ion exhange over a cationic exchange resin or by disposal of the leachate solution in the original layer of the earth frcm vzhich the contairrinaπts were derived. This represents a preferred alternative since the off nding materials are simply returned to their original place in the earth where they are largely innocuous. Ηie alkaline earth metal scales, especially barium and strontium sulfate scales and associated naturally occurring radioactive material (NORM) are removed from the earth around oil field production equipment using an aqueous scale removal ccarrpositiαn which comprises a chelating agent or chelant in combination with a catalyst or synergist. Suitable aqueous solvents or cαrpositions of this type are disclosed in the related α_pending patent application described above to which ref rence is made for a description of suitable aqueous solvent cαrrpositiαns which may be used for the removal of alkaline earth sulfate scales and NORM from surface earth formations accorxiing to the methods disclosed in this present application. Any of the scale removal compositions disclosed in the related application identified above, together with other suitable cαtpositions having the same or similar effect may be used in the present techniques and will be more or less preferred acxjording to their effectiveness. We prefer to use the oxalate cxntaimng cαrpositions, since these have been found to give fast rates of sulfate scale dissolution and are able to take up a high level of sulfate scale into solution so that they represent a particularly favored method of decontar rating surface earth formations. The mαnocarboxylic acid anion synergists especially the salicylate aniαn, have also been found to give good results, so that these too constitute a preferred class of synergists. The thiosulfate and nitriloacetate synergists are also capable of inprαving the dissolution of the scale relative to that of the chelant without the synergist. The aqueous solvent composition which is-used to remove the scale material frσm the earth c tprises a polyaitii-nopolycarboxylic acid such as ethylenediaminetetraacetic acid (EDEA) or diet_hylenetriaminepentaacetic acid (DIPA) as a chelant or chelating agent whic is intended to form a stable complex with the cation of the alkaline earth seale-forming material. Of these chelants, DIPA is the preferred species since it forms the most soluble complexes at greatest reaction rate. EDIA may be used but is scme&ftiat less favorable and, as noted below, may be less responsive to the addition of the catalyst or synergist. The chelant may be added to the solvent in the acid form or, alt__rnatively, as a salt of the acid, preferably the potassium salt. In any event the alkaline conditions used in the scale removal process will convert the free acid to the salt. The concentration of the chelant in the solvent should normally be at least O.IM in order to achieve acceptable degree of scale removal. Chelant concentrations in excess of 1.0 M are usually not necessary and concentrations from about 0.3M up to about 0.6M will normally give good results; although higher concentrations of chelant may be used, there is generally no advantage to doing so because the efficiency of the chelant utilisation will be lower at excess chelant concentrations. This economic penalty is particularly notable in oilfield operations where large volumes of solvent may be used, especially in formation scale removal treatment. In addition to the chelant, the present scale removal compositions contain a catalyst or synergist for the dissolution of the scale. As described in the expending application referred to above, the synergist is preferably the oxalate anion; a monocarboxylic anion such as mercaptoacetate, hydrαxyacetate or aminoacetate or an aromatic acid, preferably salicylate; or thiosulfate; or nitriloacetate. Generally these anions are added as salts or the free acid, depending on the stability and availability of the chosen synergist. In either case, hcwever, the relatively alkaline conditions under which the process is operated, will result in the acid, if used, being converted to the salt farm. The potassium salts are preferred in view of their greater solubility and for this reason, the solvent should preferably be brought to the desired pH value with a potassium base, preferably potassium hydroxide. The concentration of the catalyst or synergist in the aqueous solvent will be of a similar order to that of the chelant: thus, the amount of the synergist anion in the solvent should normally be at least O.IM in order to achieve a perceptible increase in the efficiency of the scale removal, and concentrations from about 0.3M up to about 0.6M will give good results. Although higher concentrations of the synergist e.g. above 1.0 M may be used, there is generally no advantage to doing so because the efficiency of the process will be lower at excess catalyst conc_entrations. Again, this ecor αic penalty is particularly notable in oilfield operations. The scale removal is effected under alkaline cxsnditions preferably at pH values of from about 8.0 to about 14.0, with optimum values being frcm about 11 to 13, preferably about 12. As noted above, the use of caustic potash is preferred to bring the cαtposition to the desired pH since the potassium salts formed by its use are more soluble than the corresponding sodium salts. The prefered solvents comprise about 0.1 to about 1.0 M of etftylεΩediaι____retetraa_etic acid (EDTA) or diethylΘ__etriaιι_in^)entaacetic acid (DIPA) , or salts of these acids, as a chelant. In addition, the chosen anionic catalyst or synergist is added to the aqueous solution in about 0.01 to about 1.0, preferably about 0.1M to 0.5 M, concentration. The pH of the solvent is then adjusted ty the addition of a base, preferably potassium hydroxide, to the desired value, preferably to about pH 12. We have found that it is important to avoid the use of sodium cations when operating at high pH values, above pH 8, and instead, to use potassium or, alternatively, cesium as the cation of the scale-removing agent. Potassium is preferred for economy as well as availability. Thus, the normal course of making up the solvent will be to dissolve the chelant and the potassium salt of the selected synergist in the water to the desired concentration, after which a potassium base, usually potassium hydroxide is added to bring the pH to the desired value of about 12. Prior to contact with the earth, the cσπposition may be heated to a temperature between about 25°C to about 100°C., in order to improve the extraction of the insoluble mineral salts, if it is readily feasible to do so. Operation in a tank or vessel may be preferred for this reason. If it is possible to control the contact time between the earth and the cαrposition e.g. by operation in a tank, the cαrposition is allowed to remain there for about ten minutes to about 7 hours; after rerraining in contact with the equipment for the desired time, the composition containing the dissolved scale may be drained off from the earth and recovered for optional removal of the dissolved scale species. The Figure shows a simplified section of the earth with an oil well extending down through the layers of the earth to a production interval from which the oil is produced. The well 10 extends through surface conductor pipe 11 and is cased through successive layers of the earth with casing of progressively decreasing diameter 12 to completion in production interval 13. The borehole extends thorough various subsurface strata S , S and S 3 , indicated conventionally in the Figure. During drilling and completion of the well, surface equipment such as drilling mast 14 with its associated equiment such as turntable, blowout preventer and pipe handling equipaient, is situated on the surface of the earth with drill pipe and tubular goods being located conveniently for installation, for example, the pipe located in pipestack 15. If subsurface waters are brought to the surface thrøjgh the well during drilling completion or production and are permitted to acx_umulate on the earth's surface, e.g. in an unlined mud pond, precipitates of the insoluble sulfate scale materials including radium may accumulate in the surface layer of the earth 16 around the well with the undesirable results referred to above. The contaminants may be removed by first applying to the surface of the earth an aqueous chemical scale removal cσπposition of the type referred to above in order to convert the insoluble alkaline earth metal sulfate precipitates to a form in which they are soluble in water. Ihe solubilized precipitates are then leached from the surface layers of the earth using additional water which is permitted to percolate into a lower level where the presence of the removed metals may be tolerated. The chemical c rposition may be applied by means of sprayers or hoses or other suitable applicators; the water may be applied in a similar manner using the same equipment if the natural rainfall at the site is sporadic or sparse. The earth surrounding the wellhead may then be returned to productive use, .Including use for agriαilture, without any potential harmful effect. As noted above, any aquifers should be protected by an overlying iirperviσus layer in order to prevent conamination of the aquifer. If the earth is decontaminated by the removal technique, the use of two separate treatment liquids, i.e. the solvent followed by water, is not necessary and it is possible to utilize one treatment only, using the aqueous, chemical solvent whic converts the sulfate precipitates to soluble form and dissolves them in the solvent itself. In the in-situ method, the use of the additional water leach is preferred in order to ensure effective removal of the precipitates with the irrinimu amount of solvent. Mineral deposits or scale derived frcm subterranean waters form on natural gas handling equipment and media such as pipework, tubing, pumps, filters, screens, and sorption media such as charcoal, silica, alumina beds, as the gas passes t_brough them and the water evaporates or is removed in the processing. The scale deposits frequently include radioactive components, especially the insoluble sulfate of radium, an alkaline earth metal, and of related metals, including thorium and thallium. The scale deposits usually include additional mineral cxπrponents, for example, the sulfates of the other metals of the alkaline earth group, especially calcium, strontium and barium, which are of low solubility in conventional solvents, as described above. Once they are formed, these scale deposits cannot be readily removed by conventional means since they are both adherent and insoluble to the conventional solvents. Thus, they cannot be readily removed by washing or other simple remedies. The deposits therefore accumulate progressively on the equipment and because many of them are radioactive because of the presence of the radioactive species, increase the activity of the equipment over a period of time until it may no longer be acceptable acxxirding to the relevant regulatory standards. According to the second aspect of the present invention, deposits of scale on gas handling equipment and media v_hich include water insoluble alkaline earth metal sulfates including radioactive contaminants such as radium sulfate, are removed ky the use of a chemical composition which includes a chelant (chelating agent) in combination with a catalyst or synergist which increases the solubility of the alkaline earth metal sulfates in aqueous solution. The preferred catalyst or synergist is the αxalate anion, but other synergists may also be used including the irono-carbαxylate acid anion and the thiosulfate or nitriloacetic acid anions, as disclosed in our copending application referred to above. Reference is made to this application for a description of suitable aqueous solvent cαrpositiαns which may be used for the removal of these scale deposits acxording to the methods disclosed in this p esent application. Any of the scale removal cαipositions i closed in the related application identified above, together with other suitable compositions having the same or similar effect may be used in the present techniques and will be more or less preferred acxxarding to their effectiveness. The aqueous solvent cαπpositiαn which is used to remove the scale material from the equipment comprises a polya_τι__nqpolycarbαxylic acid such as ethylenediam__netetraacetic acid (EDTA) or diethylenetriam__nepentaac_etic acid (DIPA) as a chelant or chelating agent which is intended to form a stable complex with the cation of the alkaline earth scale-forming material. Of these chelants, DTPA is the preferred species since it forms the most soluble complexes at greatest reaction rate. EDIA may be used but is somewhat less favorable and, as noted below, may be less responsive to the addition of the catalyst or synergist. The chelant may be added to the solvent in the acid farm or, alternatively, as a salt of the acid, preferably the potassium salt. In any event the alkaline conditions used in the scale removal process will convert the free acid to the salt. The concentration of the chelant in the solvent should normally be at least O.IM in order to achieve acceptable degree of scale removal. Chelant concentrations in excess of 1.0 M are usually not necessary and concentrations from about 0.3M up to about 0.6M will normally give good results; although higher concentrations of chelant may be used, there is generally no advantage to doing so because the efficiency of the chelant utilisation will be lower at excess chelant concentrations. In addition to the chelant, the scale removal compositions contain a catalyst or synergist for the dissolution of the scale. As described in the ccpending application referred to above, the synergist is preferably the αxalate anion; a monocarboxylic anion such as mercaptoacetate, hydrosyacetate or aminoacetate or an aromatic acid, preferably salicylate; or thiosulfate; or nitriloacetate. Generally these anions are added as salts or the free acid, depending on the stability and availability of the chosen synergist. In either case, hcwever, the relatively alkaline conditions under which the process is operated, will result in the acid, if used, being converted to the salt form. The potassium salts are preferred in view of their greater solubility and for this reason, the solvent should preferably be brought to the desired pH value with a potassium base, preferably potassium hydroxide. The pH of the solvent is adjusted by the addition of a base, preferably potassium hydroxide, to the desired value, permitting scale r moval to take place under alkaline conditions preferably at pH values of from about 8.0 to about 14.0, with optimum values being from about 11 to 13, preferably about 12. As noted above, the use of caustic potash is preferred to bring the composition to the desired pH since the potassium salts formed by its use are more soluble than the corresponding sodium salts: it is important to avoid the use of sodium cations when operating at high pH values, above pH 8, and instead, to use potassium or, alternatively, cesium as the cation of the scale-remcving agent. Potassium is preferred for economy as well as availability. Thus, the normal course of making up the solvent will be to dissolve the chelant and the potassium salt of the selected synergist in the water to the desired concentration, after which a potassium base, usually potassium hydroxide is added to bring the pH to the desired value of about 12. The concentration of the catalyst or synergist in the aqueous solvent will be of a similar order to that of the chelant: thus, the amount of the synergist anion in the solvent should normally be at least O.IM in order to achieve a perceptible increase in the efficiency of the scale removal, and (xjncentrations from about 0.3M up to about 0.6M will give good results. Although higher concentrations of the synergist e.g. above 1.0 M may be used, there is generally no advantage to doing so because the efficiency of the process will be lcwer at excess catalyst cxπicentrations. Again, this economic penalty is particularly notable in oilfield operations. In the preferred scale removal cαttpositions, a polyaminopolycarbαxylic acid such as ethylesnediaminetetraacetic acid (EDIA) or d__ethylenetr__am_u__pentaacetic acid (DIPA) is used as the chelant, preferably in an anoint of 0.1 to 1.0M as the chelant, typically about 0.5M giving good results. The preferred synergist or catalyst is the oxalate anion, as disclosed the expending application referred to above. The oxalate anion is preferably used in an amount of about 0.1 to 1.0M, preferably about 0.5M, with a pH of 10 to 14, preferably 11 to 13, and usually about 12. The desired pH value is obtained by the addition of a base, preferably a potassium base such as caustic potash, potassium hydroxide. If the chelant is added in the form of a salt, the preferred cations for the salt will be potassium since these have been found to give better solubility. An alternative synergist or catalyst is a monocarboxylic acid anion, also described in the xpending application, preferably salicylate. These anions have also been found to give fast rates of sulfate scale dissolution and are able to take up a high level of sulfate scale into solution so that they represent a particularly favored method of decontaminating gas handling equipment and media. The thiosulfate or nitriloacetic acid synergists also described in the copending application may also be used, as described in that application. The amounts of the chelant and synergist used with the moncarbojiylic acid and other synergists are ccsiparable to the amounts used with the oxalate synergists and comparable solution pH values are also used, i.e chelant and synergist concentrations frcm 0.1 to 1.0M, usually about 0.5M, solution pH from 10 to 14, usually 11 to 13 a d for best results, about 12. The scale removal composition may be heated to a temperature between about 25°C to about 100°C. (or higher if superatmospheric pressure can be employed) , in order to iπprove the dissolution of the insoluble scale species in the composition. Contact time between the equipment and the scale-removing composition is typically frcm about ten minutes to about 7 hours, depending on the thickness of the scale deposits and the tetrperature, with faster dissolution of the scale being obtained at the higher temperatures. After resrraining in contact with the equipment for the desired time, the composition containing the dissolved scale may be drained off and, if desired, recovered for removal of the dissolved scale species. In the treatment of the equipment and sorption media, the mineral deposits may be removed by washing with the selected solvent. The equipment may, if convenient, be washed with the solvent while still in place or, alternatively, removable items such as filters and minor pieces may be removed and washed with the solvent in a tank. Sorption media such as charcoal, alumina or silica, which are particulate in character, may be slurried with the solution after being unloaded from the sorption vessel or, alternatively, they may be treated in situ in the vessel if the loading of the medium and the mechanical features of the vessel permit this to be done. In either case, contact time will vary according to the thickness of the scale but at treatment temperatures of about 25° to 100° C., the duration of the treatment will normally be about 1 to 6 hours to reduce the radioac_tivity to acceptable levels. The solvent containing the dissolved scale cαrponents may then be treated to recover the dissolved radioactive materials for acceptable disposal methods, for example, by cation exchange onto a suitable cation-exchange resin to bring the radioactive components into solid form. Example Samples were taken of a charcoal gas sorption medium, which had became contaminated with radium-226, i±allium-208 and thorium 232. The samples contained these contaminants, accumulated ovear extended periods of time in gas processing, in amounts which precluded their disposal by normal methods. The activity was 24.9 pCi/g. (picocuries/gram.) for the radium component. The charcoal samples were slurried with an aqueous solution of 0.5M DIPA (diethylenetria ine pentaacetic acid) and 0.5M oxalic acid brought to pH=12 by the addition of caustic potash (potassium hydroxide) . The slurry was held at a teπperature of 90-100"C for approximately four hours, after which the charcoal was filtered off and dried. After drying, the activity of the samples was found to be 0.3 pCi/g. (radium-226) , low enough to permit disposal of the charcoal by conventional methods. Another effective chelant is cycloh__xanediam_Lnetetra- aretic acid (CDIA) , v_hich may be used with any of the synergists disclosed hereinabσve. DCEA is particularly useful with the oxalate anion at a pH of substantially 13.

Claims: CLAIMS 1. A method of decontaminating earth which has been contaminated with precipitates of alkaline earth metal sulfates, whic method comprises (i) converting the precipitated alkaline earth metal sulfates in the earth to soluble form by contacting the sulfate precipitate with an aqueous composition c___prising a chelating agent and a synergist (ii) leaching the dissolved alkaline earth precipitate frcm the earth with water. 2. A method according to claim 1 in which the earth layer is a surface earth layer contaminated with alkaline earth metal sulfate precipitate derived frcm a subsurface layer in the earth. 3. A method according to claim 1 in which the precipitates of alkaline earth metal sulfates include radium sulfate. 4. A method according to claim 1 in which the aqueous leachate is percolated into a lower layer of the earth. 5. A method acxording to claim 1 in which the contaminated earth is removed from its situs and leached in a separate location. 6. A method according to claim 5 in which the earth is leached in a tank or pond lined with an impervious l_Lning. 7. A method according to claim 5 in which the earth is separated from the leachate and returned to the approximate site from which it was removed. 8. A method acxxirding to claim 1 in vzhich the removal cαirposition comprises polyamincpolycarboxylic acid as the chelating agent and oxalate anion as a synergist. 9. A method acxording to claim 1 in which the aqueous solution comprises a polyaminopolycarboxylic acid as the chelating agent and a monocarboxylic acid anion as the synergist. 10. A method according to claim 9 in which the monocarboxylic anion is selected from hydroxyacetate, meixaptoacetate and aminoacetate. 11. A method acxording to claim 9 in which the monocarboxylic acid anion comprises salicylate anion. 12. A method accxarding to claim 1 in which the aqueous solution comprises polyaminopolycarboxylic acid as the chelating agent and a synergist selected frcm thiosulfate and nitriloacetate anions. 13. A method of decon1_aminating earth which has been contaminated with precipitates of alkaline earth metal sulfates, which method comprises (i) r__mσving the contaminated earth to a location away frcm its original site, (ii) contacting the conaminated earth conaining the precipitated alkaline earth metal sulfates with an aqueous cαtposition cαrprising a chelating agent and a .synergist to convert the alkaline earth metal sulfates to water soluble form and leach the solubilized alkaline earth metal sulfates from the earth. 14. A method according to claim 13 in which the removal cαrposition comprises polyamincpolycarboxylic acid as the chelating agent and oxalate anion as a synergist. 15. A method according to claim 13 in which the aqueous solution comprises a polyami_nopolycarboxylic acid as the chelating agent and a monocarboxylic acid anion as the synergist. 16. A method according to claim 15 in vfoich the monocarboxylic anion is selected frcm hydrαxyacetate, mercaptoacetate and aminoacetate. 17. A method acxxϊrding to claim 15 in whic the monocarboxylic acid anion comprises salicylate anion. 18. A method according to claim 13 in which the aqueous solution coπprises polyaminopolycarboxylic acid as the chelating agent and a synergist selected frcm thiosulfate and nitriloacetate anions. 19. A method of decontaminating earth which has been contaminated with precipitates of alkaline earth metal sulfates, which method comprises (i) applying an aqueous solvent composition comprising a chelating agent and a synergist to the contaminated earth at its site to convert the precipitated alkaline earth metal sulfates in the earth to soluble form, (ii) applying water to the surface of the earth treated with the solvent cσrrposition to leach the dissolved alkaline earth precipitate from the earth. 20. A method according to claim 19 in which the dissolved alkaline earth metal sulfates are leached into a lower layer of the earth. 21. A method according to claim 19 in which the removal composition comprises polyaminopolycarboxylic acid as the chelating agent and oxalate anion as a synergist. 22. A method according to claim 19 in which the aqueous solution comprises a polyami__cpolycarboxy_U.c acid as the chelating agent and a mαnocarboxylic acid anion as the synergist. 23. A method acxording to claim 22 in which the morxxarbαxylic anion is selected frcm hydrαxyacetate, mercaptoacetate and aminoacetate. 24. A method according to claim 22 in which the monocarbαxylic acid anicn comprises salicylate aniαn. 25. A method acoαrding to claim 19 in which the aqueous solution comprises polyaminopolycarboxylic acid as the chelating agent and a synergist selected frcm thiosulfate and nitriloacetate anions. 26. A method of decontaminating natural gas processing equipment and media having adherent mineral deposits of alkaline earth metal sulfates containing radioactive components, which method coπprises (i) converting the alkaline earth metal sulfates in the deposit to soluble form by contacting the deposit with an aqueous composition comprising a chelating agent and a synergist to dissolve the deposit in the cxarposition and remove it frcm the equipment. 27. A method according to claim 26 in which the removal composition comprises a polyaminopolycarboxylic acid as the cheilating agent. 28. A method according to claim 27 in which the removal composition comprises ethylenediairtijietetraacetic acid (EDIA) as the polyaminopolycarboxylic acid chelating agent. 29. A method acxxirding to claim 27 in which the removal ccmposition comprises diet_ιylenetxiam___n__pentaacetic acid (DIPA) as the polyaminopolycarboxylic acid cheϊlating agent. 30. A method according to claim 27 in which the removal ccmposition comprises a polyaιtιi__cpolycarboxylic acid as the chelating agent and oxalate anion as a synergist. 31. A method according to claim 27 in vihich the removal composition solution comprises a polyamilncpolycarboxylic acid as the chelating agent and a monocarboxylic acid anion as the synergist. 32. A method according to claim 31 in which the monocarboxylic anion is selected from hydroxyacetate, mercaptoacetate and aminoacetate. 33. A method according to claim 31, in which the monocarboxylic acid anion cαrprises salicylate anion. 34. A method according to claim 27 in vihich the removal composi ion comprises a polyaminopolycarboxylic acid as the chelating agent and a synergist selected from thiosulfate and nitriloacetate anions. 35. A method according to claim 27 in which the pH of the cαrposition is from 10 to 13. 36. A method acxording to claim 35 in which the pH of the composition is substantially 12. 37. A method according to claim 35 in which the cxmposition is brought to the specified pH by the addition of a potassium base. 38. A method according to claim 37 in which the potassium is potassium hydroxide. 39. A method according to claim 27 in which the chelating agent comprises DIPA in a concentration of from 0.1 to 1.0M. 40. A method according to claim 39 in which the synergist comprises oxalate anion in a concentration of from O.IM to 1.0M. 41. A method according to claim 40 where the pH of the solution is from 11 to 13. 42. A method according to claim 41 in which the scale is contacted with the composition at a temperature from 25°C to 100°C. 43. A method according to claim 26 in which the sulfate scale contains radium. 44. A method according to claim 26 in which a particulate gas sorption medium is contacted with the ccmposition. 45. A method according to claim 44 in which the gas sorption medium comprises charcoal, silica or alumina.

Inventors: MORRIS RICHARD L, PAUL JAMES MARK, WILSON PEGGY MAYFIELD, MORRIS, RICHARD, L., PAUL, JAMES, MARK, WILSON, PEGGY, MAYFIELD
Applicants: MOBIL OIL CORP, MOBIL OIL CORPORATION
Application year: 1990
Main classification: E02D3
IPC codes: B09C1, C02F5, C09K8, E21B43, G21F9