PREPARATION OF OVERBASED CALCIUM SULPHONATES

Abstract: The problem of sludge formation is avoided in the preparation of high base number calcium sulphonates in good yields by carbonating a mixture of: a) an oil-soluble sulphonic acid or an alkaline earth metal sulphonate, b) a hydrocarbon solvent c) a C₁₋₁₅ alcohol, preferably methanol, d) oil, and e) excess calcium hydroxide, at a temperature not exceeding 35°C, heat soaking the car­ bonated mixture, and then separating the heat soaked pro­ duct into an alcohol/water phase and a solvent/oil phase. The alcohol/water phase is removed before stripping the solvent/oil phase to yield the overbased product.

Description: PREPARATION OF OVERBASED CALCIUM SULPHONATES This invention relates to the production of overbased calcium sulphonates., and in particular to the reduction of handling problems in the preparation and processing of overbased calcium sulphonates. Overbased calcium sulphonates consist of colloidal calcium carbonate dispersed in an oil, with sulphonate acting as the surfactant. They have been known for some time as additives for automotive crankcase lubricants, their basicity neutralises acids formed in the lubricant; thereby reducing corrosion, and the dispersent effect of the additive helps to inhibit the formation of harmful deposits in the oil. Early preparations of overbased calcium sulphonates comprised first forming a gel of calcium carbonate in an aqueous medium, and thereafter dispersing the gel in a diluent oil. In US 3 105 049 calcium oxide or hydroxide is reacted with carbon dioxide in the presence of methanol to form solvated calcium carbonate, which is then mixed with an oil and a dispersant such as calcium mahogany sulphonate to gi-ve an emulsion which separates into two phases, the methanol phase being removed from the oil phase containing the dispersed product. US 3318809 describes a similar process in which finely powdered calcium oxide is slurried in methanol and carbonated in a counter - current carbonation unit before being mixed with oil and calcium sulphonate. After mixing the methanol and oil phases are separated, and following stripping the oil phase is treated with water to decompose any methanol complex. US 3 342 733 describes 2 similar process in which a colloidal gel of an alkaline earth metal carbonate in an aqueous medium is mixed with a hydrocarbon oil containing an oil-dispersable surfactant such as a calcium sulphonate to form an emulsion. The emulsion breaks on standing and the water phase is removed. "Dispersions of Insoluble Carbonates in Oilsn by Bray et al, Ind Eng Chem Prod Res Dev, Vol 14, No 4, 1975, pp 295-8 also describes that the removal of methanol by evaporation may yield a gel which is impossible to handle. Bray describes the addition of water to break this gel, but acknowledges that this may result in filtration problems. US 3 258 426 describes an alternative process for preparing calcium carbonate dispersions in oil in which an emulsion is formed of calcium carbamate in oil and the carbamate is then converted to the carbonate by heating. Coarse particles formed in the formation of calcium carbonate are retained in an emulsion which is separated from the oil phase containing the calcium carbonate dispersion. In more recent processes for preparing overbased calcium sulphonates in an attempt to produce products of higher base number (typically of 300 Total Base Number - TUBS, as measured by ASTN 2896-80) which have good stability, it is more usual to use a process in which a mixture of an oil-soluble suiphonic acid or an alkaline earth metal sulphonate, an alcohol such as methanol, calcium hydroxide and oil is carbonated, and the temperature of carbonation is reduced below the reflux temperature normally used in early calcium oxide based processes. In such processes it is also possible to employ a second solvent, typically a hydrocarbon such as toluene and/or a promoter and/or an alkaline earth metal halide. An example of such a process is given in EP 0000264, which also describes a soaking period in which, after carbonation and before stripping and filtration, the reaction mixture is held at 20 C to 35 C for at least 1/2 hour. We have found that a conventional stripping step to remove an alcohol such as methanol from the product of the low temperature carbonations of these processes tends to result in the formation of a product from which a beaver layer separates out. When the product is subsequently filtered this heavier layer forms a sludge on top of the filter cake which can tend to slow the filtering operation. The sludge has a grease-like consistency and also contains a considerable amount of the overbased calcium sulphonate product but in a form which is clearly unsuitable for use as a lubricating oil additive. This reduces the yield of usable product from the preparation. Furthermore, the accumulation of sludge presents a considerable problem in a commercial process since it requires frequent cleaning operations to keep filters and centrifuges operable, while the sludge itself presents considerable disposal problems. it has now been found that, by modifying the removal of alcohols such as methanol from the carbonated product, the tendency to sludge formation may be remarkably diminished or even eliminated. GB 2097417 describes a process for the preparation of highly basic alkaline earth metal salts in which an alkaline earth metal hydroxide is carbonated in methanol and mixed with a dispersant (as in the early prior art) but then further carbonated, and water and methanol separated from the product. However, by employing a low temperature carbonation and then separating methanol from the carbonated reaction mixture after a period of heat soaking a surprising improvement in overbased calcium sulphonate production is achieved, with reduced sediment and sludge formation resulting in improved filtration properties of the product and better yields. Moreover, the product shows advantages in viscosity and/or stability and/or haze. Thus, in one aspect the invention provides a process of preparing an overbased calcium sulphonate comprising: i) forming a mixture of a) an oil-so3uble sulphonic acid or an alkaline earth metal sulphonate, b) an aromatic or aliphatic hydrocarbon solvent, c) a C15 alcohol, d) oil, and e) an excess of calcium hydroxide over that required to react with sulphonic acid present; ii) carbonating the mixture at a temperature not exceeding 350C with from 75 to 95 wtE CO2 based on the excess calcium hydroxide; iii) heating the reaction mixture after carbon ation to a temperature not exceeding 600C over a period of not less than 15 minutes; ; iv) separating the carbonated mixture into a first phase comprising at least a major part of the alcohol and a second phase comprising at least a major part of the hydrocarbon solvent and the oil, and removing the first phase; v) removing volatile material from the second phase to yield a dispersion of overbased calcium sulphonate in oil. Component (a) of the reaction mixture includes one or more oil-soluble sulphonic acids and these may be natural or synthetic sulphonic acids, e.g. a mahogany or petroleum alkyl sulphonic acid; an alkyl sulphonic acid; or an alkaryl sulphonic acid. The alkyl suiphonic acid should preferably have at least 18 carbon atoms in the alkyl chain. Most suitable are sulphonic acids of molecular weight from 300 to 700, preferably from 400 to 500. Particularly suitable sulphonates are the alkaline earth metal salts of these most suitable suiphonic acids, and a calcium sulphonate is the preferred sulphonate. Component (a) may be conventionally used as a mineral oil solution. A suitable mineral oil solution comprises from 50 to 90E by weight, preferably 70t by weight, of sulphonic acid or sulphonate. Component (b) of the reaction mixture is an aromatic or aliphatic hydrocarbon solvent. Aromatic hydrocarbons are preferred, and examples of these are toluene, xylene and ethyl benzene. Suitable aliphatic hydrocarbons include paraffinic hydrocarbons such as n-hexane, n-heptane, n-decane, n-dodecane, white spirit, naphtha or iso-paraffins. Component (c) is very preferably methanol, although other C1 to C5 alcohols such as ethanol can be used. When component (a) is introduced as an oil solution it may be unnecessary to introduce additional oil - thus, the oil solvent for (a) acts as component (d) - and this is preferred. Alternatively oil may be introduced separately into the reaction mixture. The reaction is thus an oil solution of components (a), (b), (c) and (e). Suitable oils for component (d) include hydrocarbon oils, particularly those of mineral origin. Oils which have viscosities of 15 to 30 cSt at 380C are very suitable. Alternatively the lubricating oils described later in the specification may be used. Calcium hydroxide used as component (e) will generally be derived from a natural source such as lime or gypsum. The calcium hydroxide (component (e)) may be added in one stage or in two stages. In two stage addition first sufficient calcium hydroxide is added to neutralize the sulphonic acid, and then secondly the excess calcium hydroxide is added. However single stage addition is preferred. Additional reaction promoters may be used and these may be the ammonium carboxylates such as those described in United Kingdom patent 1 307 172 where the preferred ammonium carboxylates are those derived from C1 to C3 saturated monocarboxylic acids, e.g. formic acid, acetic acid or propionic acid. Alternatively alkali metal salts of a C1 to C3 carboxylic acid may be used, such as those of a C1 to C3 saturated monocarboxylic acid. A further alternative promoter is a metal halide or sulphide such as a halide or sulphide of an alkali metal, alkaline earth metal, aluminium, copper, iron, cobalt or nickel. Regarding the quantities of components (a), (b), (c), (d) and (e) the volume ratio of components (b) and (c) should preferably be between 30:70 and 80:20, otherwise if there is too much of component (b) the resulting product tends to be greasy, whereas with too much of component (c) the reaction mixture may tend to be too viscous during addition of carbon dioxide and any further calcium hydroxide. Preferred volume ratios of (b) and (c) are between 50:50 and 70:30. If a promoter is used we prefer to use less than 10%, e.g. between 3.08 and 7.0% by weight based on the total weight of calcium hydroxide in the reaction mixture, (i.e. including any calcium hydroxide which is added at a later stage in the reaction). The relative quantities of the other components of the reaction mixture are not so critical , but it is preferred that the weight of component (a) is 40% to 220% of the total weight of oil in the reaction mixture; and that the amounts by weight of components (b) and (c) are each between 30% and 160% of the total weight of oil, in the reaction mixture. The carbon dioxide is introduced into the mixture while it is at a temperature below 350 C, preferably not more than 30eC, and more preferably in the range to 230C to 30 C, in an amount up to from 75 to 95 wt%, preferably 80 to 90 we%, of that stoichiometrically required to neutralize the excess calcium hydroxide. When used in conjunction with the other steps of the process of the invention this low temperature carbonation promotes the reduction of sediment resulting from formation of insoluble carbonates. Very preferably step ii) comprises: ii) carbonating the mixture with an amount of from 80 to 90 wt% CO2 based on the excess calcium oxide or hydroxide at a temperature of 25 + 2 C. When the carbon dioxide has been added, if desired further calcium hydroxide, but preferably only up to the preferred maximum quantity described above, may be added and then further carbon dioxide introduced into the reaction mixture in the same manner as previously. If sulphonic acid was used initially as the component (a) it will not be necessary to use so much calcium oxide or calcium hydroxide in this second charge as was originally present in the reaction mixture before the first addition of carbon dioxide. The heating step (iii), hereinafter referred to as "a heat soak" or "heat soaking", is preferably carried out over a period of from 1/2 to 3 hours, and most preferably over 1 to 2 hours. The temperature preferably does not exceed 55eC, and more preferably does not exceed 45 CC. and most preferably in the range of 300C to 45 C. During the heat soak the reaction mixture is desirably stirred. It is believed that the heat soak results in more lime going into solution, which results in greater lime utilization and an increase TBN in the product. In addition lower viscosity products may be obtained for a given TBN. Better yields and/or a reduced skinning tendency and/or a reduction in the problems of sediment resulting from unreacted materials may also be obtained. Diluent oil may be added either to the reaction mixture following heat soaking in step iii) or to the recovered second phase of step iv) to give the required dilution to the additive product or at both stages. Addition of at least part of the oil following step iii) is believed to improve subsequent centrifugation steps. Oil is preferably added to give a product containing from 25 to 75 wt% overbased calcium sulphonate. Following heat soak, and optionally diluent oil addition, the reaction mixture is separated into two phases in step iv) and this is found to reduce the tendency to sludge formation in the product. The separation may be done by gravity - thus, by leaving the reaction mixture to stand or by mechanical means such as centrifugation or decantation in a scroll decanter This separation is preferably carried out between ambient temperature and 60 Cr more preferably at a temperature not exceeding 45 C. The first, upper layer comprises alcohol and water formed during the reaction, with possible minor amounts of the hydrocarbon solvent and neutral calcium sulphonate. The second, lower layer comprises the desired overbased calcium sulphonate in the oil with possible minor amounts of alcohol and water and any sediment. The phases are separated and the second phase is treated further to recover the desired product. The first phase may be treated to recover the alcohol, which may then be recycled. After the separation step the second phase may be heated to an elevated temperature, e.g. above 1300C, and/or reduced pressure to remove volatile materials (components (b), water and any remaining alcohol) and is preferably thereafter filtered and/or centrifuged to remove solids. Filtering may be enhanced using conventional filter aids. The desired overbased detergent additive is obtained as the filtrate. It is possible for a single centrifugation step to be employed to carry out the phase separation of step (iv) with a simultaneous solids removal. Three phase centrifuges are available capable of carrying out such a liquid-I iquid-sol id separation. The process of the invention enables a high quality, high TBN calcium sulphonate product to be obtained in good yields with reduced amounts of material losses in sludge and/or sediment and reduced problems in waste disposal which can arise when large amounts of sludge or flocculent material are produced. The process of the invention in particular provides a means of preparing a preferred product with a TBN of at least 300 mg(KOH)/g at a kinematic viscosity measured at 1000C of less than 90cSt, more preferably less than 70 cSt. More particularly, the process enables such products to be prepared such that in the final filtration of the product a preferred filtration rate of at least 200 l/hm2, more preferably at least 400 l/hm2, is achieved. In addition, preferred aspects of the process enable low haze, high stability products to be obtained. The overbased detergent of this invention is suitable for use in lubricating oils, both mineral and synthetic. The lubricating oil may be an animal, vegetable or mineral oil, for example petroleum oil fractions ranging from naphthas or spindle oil to SAE 3Q, 40 to 50 lubricating oil grades, castor oil, fish oils or oxidised mineral oil. Suitable synthetic ester lubricating oils include diesters such as di-octyl adipate, dioctyl sebacate, didecyl azelate, tridecyl adipate, didecyl succinate, didecyl glutarate and mixtures thereof. Alternatively the synthetic ester can be a polyester such as that prepared by reacting polyhydric alcohols such as trimethylolpropane and pentaerythritol with monocarboxylic acids such as butyric acid, caproic acid, caprylic acid and pelargonic acid to give the corresponding tri- and tetra-esters. Also complex esters may be used as base oils such as those formed by esterification reactions between a dicarboxylic acid, a glycol and an alcohol and/or a monocarboxylic acid. Blends of diesters with minor proportions of one or more thickening agents may also be used as lubricants. Thus one may use blends containing up to 508 by volume of one or more water-insoluble polyoxyalkylene glycols, for example polyethylene or polypropylene glycol, or mixed oxyethylene/oxypropylene glycol. The amount of overbased detergent added to the lubricating oil should be a minor proportion , e.g. between 0.01% and 10% by weight, preferably between 0.1E and 5E by weight. The final lubricating oil may contain other additives according to the particular use for the oil. For example, viscosity index improvers such as ethylene propylene copolymers may be present as may succinic acid based dispersants, other metal containing dispersant additives and the well known zinc dialkyldithiophosphate antiwear additives. The invention extends to an additive concen- trate comprising an oil solution of an overbased calcium sulphonate of the invention and preferably one or more additional additives. It also extends to a lubricating oil containing the overbased calcium sulphonate. The present invention is now described, though only by way of illustration, by reference to the following Examples. Comparative Examples A to J and Examples 1 to 6 In these Examples, unless otherwise indicated, the initial reaction mixture comprising reactants in the following proportions, based on a five litre laboratory scale test comprised: Toluene 1353g Sulphonic acid 1) 1353g Methanol 812g Lime 2) 793g Notes: 1) an oil solution containing 68.5 wtt active ingredient of 480 average molecular weight of which 258 is a C18 straight chain sulphonic acid and 75t is a C24 propylene oligomer sulphonic acid. 2) Lime obtained from Balthazard et Cotte of France which contains 95 wt% calcium hydroxide, and approximately 0.3 wt% magnesium in the carbonation step, unless otherwise indicated, the amount of carbon dioxide added to the above mixture was 356g - i.e. 88 wtZ of the stoichiometric amount required by the overbasing amount of lime - charged over 3.64 hours. Where different amounts are added the overall charge time for CO2 is the same. Diluent oil is added to the carbonated product, unless otherwise indicated, in an amount of 875g. Stanco 150 is used as the diluent oil Comparative Example A a) Charging: The sulphonic acid and toluene were charged to a reactor fitted with a reflux condenser, stirrer and sparge tube, and stirred. The methanol was added, and then the lime. The temperature rose to 35to, and the reactor was cooled to 25 + 2 C. b) Carbonation: Carbonation commenced at a rate of 97.8gZhour CO2, and the temperature was maintained at 25 + 20C until 698 CO2 was added. Then the temperature was raised to 550C over the remaining carbonation time. c) Stripping: A nitrogen sparge was commenced and the reflux condenser replaced by a take-off condenser. The temperature was then raised to 80 C. Diluent oil was added during stripping at the rate that material was distilled off. The mixture was then centrifuged, and the centrifugate further stripped under vacuum at 1500C. d) Filtration: The stripped product was filtered using Dicalite Special Speedflow filter aid (available from General Refractory Co. of USA) as precoat and either 2% Speedplus or 2% Speedex (both available from General Refractory Co.) as an admix. Other filter aids used as admixes in the following Examples as shown in the Table. For Comparative Examples B to J and Examples 1 to 6 the procedure was as described for Comparative Example A except where variations are shown in Table 1 below. TABLE 1 A B C D E Charging Lime addition one one one one two (stages) (over 1 hour) (over 1 hour) (30 min + 10 min) Carbonation Temperature ( C) 25-55 25-55 25-55 25-55 25-30 % Stoichiometric 88 88 88 88 88 CO2 Heat Soak Temperature ( C) - - - - Time (hour) - - - - Phase Separation No No Gravity Gravity Gravity Stripping Temperature ( C) 80 150 150 - 150 Centrifuge Yes Yes Yes Yes Yes Temperature ( C) 150 - - Thin film evaporator Filtration SSF precoat + (i) +2% SPLUS (i) 2% SPLUS 2.5% SSF 1.5% SSF 3.0% SSF admix *(%) ii) +2% SDX (ii) 2% SDX *SPLUS = Speedplus SDX = Speedx SSF = Sp Speedflow TABLE 1 F G H I J 1 Charging Lime addition two two two one one one (stages) (30 min + 10 min) (30 min + 10 min) (30 min + 10 min) (over 1 hour) (1 hours) (1 hour) Carbonation Temperature ( C) 25-30 25-30 25-30 25-55 25-55 25-30 % Stoichiometric 88 92 96 88 88 88 CO2 Heat Soak Temperature ( C) - - - - 55 30-55 Time (hour) - - - - 1 1 Phase Separation Gravity Gravity Gravity Gravity Gravity Gravity Stripping Temperature ( C) - 150 150 - - Centrifuge Yes Yes Yes Yes Yes Yes Temperature ( C) Thin film - - 150 150 150 evaporator Filtration SSF precoat 3.0% SSF 1.5% SSF 3.0% SSF (i)1.5% SSF (i) 1.5% SSF 1.5%SSF admix (%) (ii)3.0% SSF (ii) 3.0% SSF TABLE 1 2 3 4 5 6 Charging Lime addition one one one one two (1 hour) (1 hour) (1 hour) (1 hour) (30 min + 30 min) Carbonation Temperature ( C) 25-30 25-30 25-30 25-30 25-30 % Stoichiometric 88 92 92 92 88 CO2 Heat Soak Temperature ( C) 30-55 30-55 30-55 30-55 30-55 Time (hour) 1 1 1 1 1 Phase Separation Gravity Gravity Gravity Gravity Gravity Stripping Temperature ( C) 80 150 150 - 150 Centrifuge Yes Yes Yes Yes Yes Temperature ( C) 150 150 150 - 150 Filtration SSF precoat + 1.5% SSF (i) 1.5% SSF 3.0% SSF (i) 1.5% SSF (i) 1.5% SSF admix (%) (ii) 3.0% SSF (ii) 3.0% SSF The results of the above Examples and- Comparative- Examples are given in Table 2 below which indicates the analysis of the overbased calcium sulphonate product, and the amounts of sediment and sludge formed at various stages in carrying out the preparation. Also given are the critical processing parameters of filterability and centrifugate flow rate which indicate how readily the desired product may be isolated. The process of the invention shows a remarkable reduction in the sludge formation, which gives a more efficient process with less processing problems and a greater yield of the desired product. In this connection it is pointed out that the term "sludge" is used to describe a heavy layer formed within the product which is hazy in appearance and has a grease-like consistency when filtered off the product. It is to be distinguished from particulate sediments which generally comprise calcium carbonate and/or neutral calcium sulphonate and which.are deposited from the product as hard or soft precipitates. On filtering the sediments form a filter cake, while any sludge is deposited as a greasy layer on top. The analytical results given are measured on the filtrate diluted to a nominal 300 TBN with diluent oil, unless otherwise indicated. Kinematic viscosity was measured at 100etc by the technique described in ASTM D445-79. The soap content was measured by the technique described in ASTM D3712 Foaming tendency was measured on a solution of 2.0 wt% of the filtrate in diluent oil by the technique described in ASTM Due92 Seq I using 400 ppm of Dow Corning D200 silicone as anti-foaming agent, unless otherwise indicated. Blend stability was measured by observing a) the volume percentage of sediment formed after mixing the sample with heptane in a 1:1 (v/v) ratio and centrifuging for 20 minutes; and (b) the volume percentage of sediment formed after the sample/heptane mixture is left to stand for 24 hours. Example A B C Process Results Units After sediment Vol % 1.6 1.6 2.0 carbonation sludge Vol % - - ---------------------------------------------------------------------------------------------------------------------- After sedinent Vol % 0.12 0.8 3.0 stripping sludge Vol % 8.0 6.0 1.0 ---------------------------------------------------------------------------------------------------------------------- After sediment Vol % 0.06 0.3 centrifugation sludge Vol % 0.1 6.0 ---------------------------------------------------------------------------------------------------------------------- Centrifugate flow rate g/min 220 220 ---------------------------------------------------------------------------------------------------------------------- Filterability* 1/hm2 i) 69 i) 0 102 ii)102 ii) 0 ---------------------------------------------------------------------------------------------------------------------- Analytical Results Total base no. mgk08/g 325.0 325.0 354.9 326.9 326.9 ---------------------------------------------------------------------------------------------------------------------- Kinematic vis- cSt 62.1 67.7 253.8 (TBN 354.9) cosity at 100 C 49.3 (TBN 300) ---------------------------------------------------------------------------------------------------------------------- % soap mass % 35.8 ---------------------------------------------------------------------------------------------------------------------- % calcium mass % 14.3 ---------------------------------------------------------------------------------------------------------------------- Water plus mass % 35.8 solvent content ---------------------------------------------------------------------------------------------------------------------- Foaming tendency ml/ml 0-0 (TPN 300) 49.5-30 (No. A/F) ---------------------------------------------------------------------------------------------------------------------- Blend stability vol % 0.4/1.0 (initial/24 hr sediment) ----------------------------------------------------------------------------------------------------------------------- Example D E F Process Results Units After sediment Vol % 2.0 3.0 3.0 carbonation sludge Vol % - - ----------------------------------------------------------------------------------------------------------------------- After sediment Vol % 0.2 3.0 0.2 stripping sludge Vol % trace none none ----------------------------------------------------------------------------------------------------------------------- After sediment Vol % - centrifugation sludge Vol % - - ----------------------------------------------------------------------------------------------------------------------- Centrifugate flow rate g/min 250 - 200 ----------------------------------------------------------------------------------------------------------------------- Filterability 1/hm2 33 0 35 ----------------------------------------------------------------------------------------------------------------------- Analytical Results Total base no. mgkOH/g 315.8 326.2 296.0 ----------------------------------------------------------------------------------------------------------------------- Kinematic cSt 55.5 166.1 178.2 viscosity at 100 C ----------------------------------------------------------------------------------------------------------------------- % soap mass % - 32.3 28.4 ----------------------------------------------------------------------------------------------------------------------- % caicium mass % - 12.89 11.86 ----------------------------------------------------------------------------------------------------------------------- Water plus mass % - - 2.40 solvent content ----------------------------------------------------------------------------------------------------------------------- Foaming tendency ml/ml - - 190-90 (No A/F) ----------------------------------------------------------------------------------------------------------------------------- Blend stability Vol % 0.5/1.8 1.8/1.4 (initial /24 bra sediment) ------------------------------------------------------------------------------------------------------------------------- Example G H I Process Results Units After sediment Vol % 3.8 1.8 1.2 carbonation sludge Vol % none none none --------------------------------------------------------------------------------------------------------------------------------- After sediment Vol % 0.2 0.3 0.1 hard/0.1 seft stripping sludge Vol % none none none --------------------------------------------------------------------------------------------------------------------------------- After sediment Vol % 0.08 + 0.01 Gel 0.1 Centrifugation sludge Vol % none none --------------------------------------------------------------------------------------------------------------------------------- Centrifugate flow rate g/min 180 105 Filterability 1/hm2 67 55 i) 47 ii) > 119 iii) > 142 --------------------------------------------------------------------------------------------------------------------------------- Analytical Results Total base no. mgkOH/g 308.3 317.1 327 --------------------------------------------------------------------------------------------------------------------------------- Kinematic viscosity cSt 166.1 at 100 C --------------------------------------------------------------------------------------------------------------------------------- % soap mass % 31.4 30.3 30.8 --------------------------------------------------------------------------------------------------------------------------------- % calcium mass % 12.56 12.55 12.77 --------------------------------------------------------------------------------------------------------------------------------- Water plus mass % solvent content --------------------------------------------------------------------------------------------------------------------------------- Foaming tendency ml/ml 0-0 0-0 0-0 --------------------------------------------------------------------------------------------------------------------------------- Blend stability vol % 0.4/1.4 0.4/1/6 0.14/0.40 (initial/24 hr sediment) ---------------------------------------------------------------------------------------------------------------------------------- Example J 1 2 Process Results Untis After sediment Vol % 0.8 3.0 2.0 carbcnation sludge Vol % none (0.8 after heat up) (0.8 ater heat up) ------------------------------------------------------------------------------------------------------------------------------------------- Ater sediment Vol % 0.3 0.04 hard/0.15 soft 0.8 stripping sludge Vol % none none none ------------------------------------------------------------------------------------------------------------------------------------------- Ater sediment Vol % - 0.02 hard/0.02 soft Centrifugation sludge Vol % none none none ------------------------------------------------------------------------------------------------------------------------------------------- Centrifugate flow rate g/min - - 80 ------------------------------------------------------------------------------------------------------------------------------------------- Filterability 1/bm2 i) 33 476 i) 35 ii) 40 ii) 102 iii) 51 ------------------------------------------------------------------------------------------------------------------------------------------- Analytical Results Total base no. mgkOH/g 324.5 325.0 324.0 ------------------------------------------------------------------------------------------------------------------------------------------- Kinematic cSt 178.2 44.4 57.5 viscosity at 100 C ------------------------------------------------------------------------------------------------------------------------------------------- % soap mass % 30.1 30.1 29.9 ------------------------------------------------------------------------------------------------------------------------------------------- % calcium mass % 12.99 13.04 12.93 ------------------------------------------------------------------------------------------------------------------------------------------- Water plus mass % 0.52 0.30 0.60 solvent content ------------------------------------------------------------------------------------------------------------------------------------------- Foaming tendency ml/ml 0-0 0-0 0-0 ------------------------------------------------------------------------------------------------------------------------------------------- Blend stability vol % 0.002/0.10 0.3/0.4 0.2/0.3 (initial/24 hr sediment) -------------------------------------------------------------------------------------------------------------------------------------------- Example 3 4 5 Process Results Units After sediment Vol % 2.8 2.8 2.8 carbonation sludge Vol % none none none ------------------------------------------------------------------------------------------------------------------------------------------ After sediment Vol % 0.50% hard N/A N/A stripping sludge Vol % none ------------------------------------------------------------------------------------------------------------------------------------------ After sediment Vol % - - 0.02 hard/0.10 soft Centrifagation sludge Vol % - - none ------------------------------------------------------------------------------------------------------------------------------------------ Centrifugate flow rate g/min - - 120-140 ------------------------------------------------------------------------------------------------------------------------------------------ Filterability 1/hm2 i) 286 93 107 ii) 274 ------------------------------------------------------------------------------------------------------------------------------------------ Analytical Results Total base no. mgkOH/g 333.6 - ------------------------------------------------------------------------------------------------------------------------------------------ Kinematic visoosity cSt - - at 100 C ------------------------------------------------------------------------------------------------------------------------------------------ % soap mass % 31.5 30.3 32.0 ------------------------------------------------------------------------------------------------------------------------------------------ % calcium mass % 13.17 13.05 13.14 ------------------------------------------------------------------------------------------------------------------------------------------ Water plus mass % 0.66 1.08 0.8 solvent content ------------------------------------------------------------------------------------------------------------------------------------------ Foaming tendency ml/ml 230-40 (No. A/F) 210-40 (No. A/F) 180-40 (No. a/F) ------------------------------------------------------------------------------------------------------------------------------------------ Blend staoility vol % 0.4/1.8 0.2/0.10 after 3 days 0.9/1.2 (intial/24 br sediment) ------------------------------------------------------------------------------------------------------------------------------------------- Example 6 Process Results Units After sediment Vol % 1.0 carbonation sludge Vol % none After sediment Vol % 0.3 soft stripping sludge Vol t none After sediment Vol % 0.3 Centrifugation sludge Vol % none Centrifugate g/min 120 flow rate Filterability 1/hmê i) 57 ii) 71 Analytical Results Total base no. mgkOH/g 306.0 Kinematic cSt 50.6 viscosity at 100 C E soap mass t 8 calcium mass % Water plus mass % solvent content Foaming tendency ml/ml Blend stability vol % 0.20/0.6 (initial/24 hr sediment) Comparative Examples A and B which do not employ a phase separation step form significant amounts of sludge. Comparative Examples C and D use a phase separation step but in conjunction with a high temperature carbonation, and the product still contains some sludge, has poor filterability and poor blend stability. Comparative Examples E-J show no sludge formation but the products have poor filterability and/or poor blend stability and/or high viscosity. Comparative Example J includes both phase separation and heat soaking step but employs a high temperature carbonation. The results are to be compared to those for Example 1, which is a similar process except that the low temperature conditions of the invention are employed. Whereas Comparative Example J gives poor filterability and an unacceptably high viscosity, Example 1 gives excellent filterability and a much lower viscosity. Examples 2 to 6 show the effect of variations from the preferred procedure of Example 1; in each case the product is free from sludge and where measured the viscosity is much lower than Comparative Example J. Examples 2 and 4 show reduced filterability but these results were obtained without a centrifugation step between phase separation and filtering and this would be expected to make filtration difficult. Examples 3 to 5 also show that carbonation beyond 90% of stochiometric results in a less optimum product, and Example 6 shows that two part lime is less advantageous but the product of this Example shows improved blend stability as compared to Comparative Examples E-H which also use two part lime addition. Examples 7 to 11 A further set of experiments was carried out using the same reactants as in the previous Examples, but on a 3 litre scale in the following amounts: Toluene 812g Suiphonic Acid 812g Methanol 487g Lime 476g The following procedure was employed: a) Charging: The sulphonic acid and toluene were charged to a reactor fitted with a reflux condenser, stirrer and sparge tube, and stirred. The methanol was added, and then the lime. The temperature rose to 35 C, and the reactor was cooled to 25 + 2 C. b) Carbonation: Carbonation was conducted at 25 + 20C over 3.5 hours so that carbon dioxide was adsorbed to 90% of the stoichiometric amount required by the overbasing lime. c) Heat soak: The carbonated mixture was stirred at the temperatures and for the times shown in Table 3 below. d) Diluent oil addition: 525g of diluent oil were then added to the heat soaked product. e) Phase separation: The mixture was separated by centrifuging into a first liquid phase comprising a major part of the methanol, a second liquid phase comprising small amounts of solid phase which is discarded. f) Stripping: The second liquid phase was stripped by heating to 1600C under vacuum over 2 hours and then maintaining under vacuum at a temperature of 1600C for a further 2 hours. g) Filtration: The stripped product was filtered using Dicalite Special Speedflow filter aid as precoat and 1.5% Special Speedflow as an admix. The analysis of the material was carried out as described hereinbefore with the addition of a haze test. Haze was measured as the amount of light scattering determined using a nephalometer (Coleman Photonephelometer available from Coleman Instruments Company of USA). The measurements are carried out on a Swt% solution in diluent oil and the results are expressed in nephalos. TABLE 3 Example 7 8 9 10 11 Heat Soak Temperature ( C) 25+40 25 25+40 25+40 40 Time (hours) 1.0+1.5 2.0 2.0+0.5 2.0+1.0 1.5 Process results After stripping sediment (vol %) 0.07 0.08 0.05 0.06 0.06 sludge (vol %) none none none none none Filterability (l/hmê) 394 488 396 485 327 Product Analysis TBN (mgKOH/g) 333 323 336 334 332 kV at 100 C (cSt) 69.5 83.2 62.4 71.5 71.5 Stability trace/0.02 0.02/0.02 0.05/0.02 trace/trace 0.01/0.02 (initial/24hr sediment) (vol%) Foaming tendency (ml/ml) 0/0 0/0 0/0 0/0 0/0 Haze (nephalos) 58 60 68 66 58 Example 12 The procedure of Examples 7 to 11 was repeated except for the following changes: Reactants: Lime from Company of USA US Gypsum was used in place of lime from Balthazard et Cotte. b) Carbonation Carbonatipn was carried out over 3 hours, but still to 90% of the stoichiometric amount required by the overbasing lime. c) Heat Soak This was conducted at 4000 for 1.5 hours. Six repeats were made of this test and the results in Table 4 below represent the average of the six runs. TABLE 4 Process Results After stripping sediment (vol %) 0.10 sludge (vol %) none Filterability tlZhm2) 625 Product Analysis TEN (mgKOH/g) 335 kV at 10000 (cSt) 60.8 Stability < 0.005/ < 0.01 (initial/24hr sediment) (vol%) Foaming tendency (ml/ml) 0/0 Haze (nephalos) 16 Example 13 The procedure of Example 12 was repeated except for the following change: a) Charging: The lime, most of the toluene and methanol were charged to the reactor, and then the sulphonic acid and remaining toluene was added. The reactor was cooled to 25+2°C. Again six repeats were carried out and the results are given in Table 5 below. TABLE 5 Process Results After stripping sediment (vol t) 0.1 sludge (vol E) none Filterability (l/hm2) 806 Product Analy is TBN (mgKOH/g) 333 kV at 100etc (cSt) 61.7 Stability < 0.01/ < 0.02 (initial/24hr sediment) (vol%) Foaming tendency (ml/ml) 0/D Haze (nephalos) 17 Example 14 and Comparative Examples K and L The procedure of Example 12 was repeated using Balthazard Lime in place of US Gypsum lime. To provide a comparison this preparation was repeated without heat soaking (Comparative Example K) and without phase separation (Comparative Example L ) . The results are given in Table 6 below. TABLE 6 EXAMPLE 14 K L Process Results After stripping sediment (vol %) 0.1 0.15 2.0 sludge (vol 9s ) none none none Filterability (l/hm2) 218 592 17 Product Analysis (mgKOH/g) 332 299 334 kV at 1000C (cSt) 73.1 138.7 insufficient Stability (0.02/-) trace/trace product available (initial/24hr sediment)(vol%) after filtration Foaming tendency (ml/ml ) 0/0 0/0 0/0 Haze (nephalos) 58 12 22 The results show that the process of the invention is advantageous in terms of giving a sludge-free product which is readily filtered, and shows high product quality in terms of TBN, viscosity, stability, foaming tendency and haze. In Comparative Example K the absence of a heat soak step leads to a low TBN product with high viscosity indicating a less efficient overbasing process. This product would be unsuitable for use as a 300TBN additive in view of its unacceptably high viscosity. Comparative Example L shows that the omission of the phase separation step results in such a low filtration rate that product yield was minimal. A large amount of sediment was also formed. Such a process would be impractical for preparation of an additive on a commercial scale.

Claims: CLAIMS 1. A process of preparing an overbased calcium sulphonate comprising: i) forming a mixture of a) an oil-soluble sulphonic acid or an alkaline earth metal sulphonate, b) an aromatic or aliphatic hydrocarbon solvent, c) a C15 alcohol, d) oil, and e) an excess of calcium hydroxide over that required to react with sulphonic acid present; ii) carbonating the mixture at a temperature not exceeding 35 C with from 75 to 95 wt% CO2 based on the excess calcium hydroxide; iii) heating the reaction mixture after carbonation to a temperature not exceeding 600C over a period o±.not le-ss than 15 minutes. iv) separating the carbonate mixture into a first phase comprising at least a major part of of the alcohol and a second phase comprising at least a major part of the hydrocarbon solvent and the oil, and removing the first phase; v) removing volatile material from the secorid phase to yield a dispersion of overbased calcium sulphonate in oil. 2 A process as claimed in claim 1, in which step ii) comprises: ii) carbonating the mixture at a temperature of not exceeding 30 C. 3 A process as claimed in claim 1 or claim 2, in which diluent oil is added following step iii) and/or following step v) 4 A process as claimed in any of claims 1 to 3, in which in step iii) the carbonated reaction mixture is heated to a temperature not exceeding 550C for 1/2 to 3 hours. 5 A process as claimed in claim 4, in which the carbonated reaction mixture is heated to from 300C to 45 C. 6. An overbased calcium sulphonate whenever prepared by a process as claimed in any of claims 1 to 5, and having a total base number (as defined herein) of at least 300. 7 An overbased calcium sulphonate as claimed in claim 6, having a viscosity measured at 1000C and a total base number of 300 of less than 90 cSt. 8. The use of an overbased calcium sulphonate as claimed in claim 6 or claim 7 as a lubricating oil additive. 9. A lubricating oil comprising an overbased calcium sulphonate as claimed in claim 6 or claim 7. 10 An additive concentrate for blending with lubricating oil comprising an oil solution of an overbased calcium sulphonate as claimed in claim 6 or claim 7.

Inventors: ALCOCK, KENNETH
Applicants: EXXON RESEARCH AND ENGINEERING COMPANY
Application year: 1983
Main classification: C10M135
IPC codes: C10N40, C07C67, C10N10, C10M159, C07C301, C07C309, C10N20, C10N70, C10N30