CA1335895C

CA1335895C - Low temperature method for the production of long chain hydrocarbyl substituted mono- or dicarboxylic acid materials employing plural zone mixing

Info

Publication number: CA1335895C
Application number: CA 590329
Authority: CA
Inventors: Renee Marie Roper; Jai Gopal Bansal; Oon Chee Nong; Jacob Emert
Original assignee: Exxon Chemical Patents Inc
Current assignee: ExxonMobil Chemical Patents Inc
Priority date: 1989-02-07
Filing date: 1989-02-07
Publication date: 1995-06-13
Anticipated expiration: 2012-06-13

Abstract

The present invention provides a process for the preparation of long chain hydrocarbyl substituted mono- or dicarboxylic acid materials in high active ingredient concentrations which comprises reacting a long chain hydrocarbon polymer, generally a polyolefin, and an monounsaturated carboxylic reactant such as maleic anhydride in the presence of chlorine, wherein at least about 60 mol% of the chlorine is added to the reaction mixture containing said polyolefin and monounsaturated carboxylic reactant at a reaction temperature not greater than about 170°C while imparting to the reaction mixture a total mixing energy of at least about 4 HP/1000 gal. A
reaction zone provided with plural zone mixing comprising at least one axial pumping mixing zone and at least one high shear mixing zone is employed. This process selectivity produces more monofunctionalized long chain hydrocarbyl substituted mono- or dicarboxylic acid material product and substantially reduces the amount of oxidized by-product material, giving less sediment to be removed from the product.

Description

, 133~8s$

IMPROVED LOW TEMPERATURE METHOD FOR THE PRODUCTION OF
LONG CHAIN HYDROCARBYL SUB~lllul~D MONO- OR DICARBOXYLIC
ACID MATERIALS EMPLOYING PLURAL ZONE MIXING (PT-711) FIELD OF THE INVENTION

This instant invention relates to a process for the preparation of long chain hydrocarbyl substituted mono-and dicarboxylic acid materials. More particularly, the process involves the reaction of a long chain hydrocarbon polymer, generally a polyolefin, with an ethylenically unsaturated mono- or dicarboxylic acid material such as maleic anhydride or acrylic acid in the presence of chlorine. Copending application S.N. 590,328 deals with related subject matter.
BACKGROUND OF THE INVENTION

High molecular weight or long chain hydrocarbyl substituted dicarboxylic acid materials such as polyisobutenyl substituted succinic anhydrides are well known in the art and have many important industrial uses.
For example, they are useful as additives in lubricants and fuels and as intermediates in the preparation of additives such as dispersants for lubricants and fuels. They can be prepared by thermally reacting long chain hydrocarbon polymers, generally polyolefins (such as polyisobutylene), with ethylenically unsaturated dicarboxylic acid materials such as maleic anhydride at temperatures in excess of about 200C. However, this reaction suffers from a relatively low degree of conversion and if an attempt is made to improve the degree of conversion by increasing the temperature or pressure, an undesirable degradation of maleic anhydride occurs with resulting formation of carbon mono- and dioxide, water and solids. For this reason, ,,' ~

resort has been made to initial preparation of a halogenated hydrocarbon reactant followed by reaction of the halogenated hydrocarbon with maleic anhydride.
However, this reaction has several drawbacks. A principal drawback is that it requires a first step of halogenating a hydrocarbon and a second step of reacting maleic anhydride with the halogenated hydrocarbon so obtained. Both steps are slow so that the overall process is extremely time-consuming.
Alternatives to this halogenation process are processes which involve the use of halogen such as chlorine, to facilitate attachment of maleic anhydride to the hydrocarbon such as a polyolefin backbone. The following patents describe such alternative processes.
U.S. Patent Nos. 3,215,707 and 3,231,587 disclose a process for the preparation of hydrocarbon-substituted succinic acids and derivatives thereof involving preparing a miXture of an olefin polymer and maleic anhydride, and contaating said mixture at a temperature above about 140C
with at least about one mole of chlorine for each mole of maleic anhydride. The patentee indicates that it is critically important that the C12 be introduced into the reaction mixture after the olefin polymer has been throroughly mixed with the maleic anhydride. The preferred temperatures are disclosed as ranging between about 160C
and about 220C and even higher, e.g., 250C. Example 6 of these patents discloses the reaction of a polyisobutene having a molecular weight of 1000 with maleic anhydride and chlorine at 155C comprising a series of discrete sequential additions of mixing maleic anhydride with, and bubbling chlorine to, the reaction mixture containing polyisobutene.
U.S. Patent No. 3,755,169 discloses a process for preparing high molecular weight polycarboxylic acid acylating agents by intimately contacting chlorine with a - - j ~ 3 ~ 133~895 reaction mixture comprising (1) high molecular weight monocarboxylic acid and ethylenically unsaturated low molecular weight mono- or polycarboxylic acid acylating agent or (2) high molecular weight aliphatic hydrocarbon, ethylenically unsaturated low molecular weight monocarboxylic acid acylating agent, and ethylenically unsaturated low molecular weight polycarboxylic acid acylating agent. This patent discloses that the reaction mixture is contacted with chlorine at a temperature of at least about 140-C, the maximum temperature being critical only to the extent that it should not exceed the minimum decomposition temperature of any member of the reaction mixture or of the products produced. This patent further disclases that ordinarily, temperatures will not exceed 300C and preferably will be in the range of about 160C to about 260C. Examples of the patentees' method are illustrated in which the C12 gas is introduced into the liquid reaction mixture through a subsurface inlet in a reaction vessel equipped with a reflux condenser.
U.S. Patent No. 3,912,764 discloses a two-stage process for preparing alkenyl succinic anhydrides in which in the first stage a thermal reaction between the olefin polymer and maleic anhydride is carried out to a point short of complete reaction of all of the maleic anhydride and the reaction is then continued in a second stage in the presence of a small amount of chlorine, less than 1 mole of chlorine for each mole of maleic anhydride then present in the reaction mass, until the remaining maleic anhydride is substantially used up. In the first stage the olefin polymer and maleic anhydride are throughly mixed and the mixture's temperature is raised to a reaction temperature in the range of 180C to 250-C, preferably in the range of 200 - 230C. In the second stage the reaction temper-atures may be in the range of from 160C to 225C, preferably from 165C to 200-C.

_ 4 _ 133S895 U.K. Patent No. 1,543,039 discloses a process for the preparation of polyisobutene-substituted succinic anhydride whereby higher polymer conversions to lower chlorine containing products may be obtained. This process comprises preparing a mixture of maleic anhydride and a polymer of isobutene and contacting the mixture with a molar deficiency of chlorine based on maleic anhydride, i.e., 0.3 to 0.95 moles of chlorine for each mole of maleic anhydride, before half of the maleic anhydride has reacted. The reaction temperatures are disclosed as varying between wide limits, with temperatures in the range of from 140 to 220C being suitable, and those from 160 to 210C being preferred.
U.S. Patent No. 3,868,330 discloses a process for preparing high molecular weight polycarboxylic acid acylating agents by contacting chlorine with a reaction mixture comprising (I)(A) high molecular weight monocarboxylic acid and (B) ethylenically unsaturated low molecular weight mono- or polycarboxylic acid acylating agent or (II)(c) high molecular weight aliphatic hydrocarbon, (D) ethylenically unsaturated low molecular weight mono-carboxylic acid acylating agent, and (E) ethylenically unsaturated low molecular weight polycarboxylic acid acylating agent. The reaction temperature is disclosed as being at least 140C, with the maximum temperature being critical only to the extent that it should not exceed the minimum decomposition temperature of any member of the reaction mixture or of the products produced. Ordinarily, temperatures will not exceed 300C
and preferably are in the range of about 160C to about 260C. The amount of chlorine used in reaction mixture I
is that which will provide at least about 0.8, preferably at least about one, mole of chlorine per mole of (B), and in reaction mixture II at least about 0.8 and preferably at least about one mole of chlorine for each mole of the total number of moles of (D) and (E).

U.S. Patent 4,110,349 discloses a two-step process for the preparation of substituted carboxylic acids and their derivatives comprising: (I) reacting (A) at least one alkylating hydrocarbon with an amount of (B) at least one of maleic acid, fumaric acid, itaconic acid, and anhydrides and esters of any of these acids equal to about 30-90% by weight of the amount required to afford the desired product, in the presence of about 0-0.4 mole of chlorine per mole of (B); and subsequently (II) introducing additional (B) sufficient to afford the desired product and continuing the reaction in the presence of added chlorine, the amount of said added chlorine being up to about 4 moles per mole of said additional (B). The reaction temperature is disclosed as being in the order of lOO-C - 250C, and it is preferred that the temperature be at least about 150-C
during most of step I. The reaction temperatures for step II are disclosed as being generally within the range of about 100-250C, with 170-225C being preferred.
U.K. Patent 1,492,337 discloses a process for preparing substituted succinic acid acylating agents which comprises:
(I) preparing an initial admixture of (A) at least one substantially aliphatic polymer of at least one lower olefin, which polymer contains at least 30 aliphatic carbon atoms, and (B) an acidic reactant selected from fumaric acid; itaconic acid; the lower alkyl esters, acyl chlorides, and acyl bromides of either of these acids; maleic anhydride; itaconic anhydride and a compound corresponding to the formula ~o CH - C R
CH C R' ~ O

wherein R and R' are each independently selected from -OH, -O-, lower alkyl, -Cl and -Br; and mixtures of two or more of any of these acid reactants, and (II) heating said initial admixture to a temperature of at least 100-C, introducing chlorine into the heated admixture, and increasing the temperature of the resulting reaction mixture to at least 190C, the total amount of chlorine introduced being from 0.4 to 0.9 mole of chlorine for each mole of acidic reactant in said initial admixture.
U.S. Patent No. 4,234,435 discloses several processes for the preparation of substituted succinic acylating agents. One process, a two-step chlorination procedure, involves first chlorinating a polyalkylene until there is an average of at least about one chloro group for each molecular weight of polyalkylene. Chlorination involves contacting the polyalkylene with chlorine gas until the desired amount of chlorine is incorporated into the ahlorinated polyalkene. Chlorination is generally carried out at a temperature of about 75C to about 125C.
The second step is to react the chlorinated polyalkene with the maleic reactant at a temperature usually within the range of about 100C to about 200C. The mole ratio of chlorinated polyalkene to maleic reactant is usually about 1:1. However, a stoichiometric excess of maleic reactant can be used, for example, a mole ratio of 1:2. Another process disclosed in this patent is one wherein the - 7 - 1 33~ 895 polyAlkene and the maleic reactant are first reacted by heating them together in a "direct alkylation" procedure.
When the direct alkylation step is completed, chlorine is introduced into the reaction mixture to promote reaction of the remaining unreacted maleic reactants. In this process 0.3 to 2 or more moles of maleic anhydride are used in the reaction for each mole of olefin polymer, i.e., polyalkene. The direct alkylation step is conducted at temperatures of 180C to 250C. During the chlorine introducing stage a temperature of 180C to 225-C is employed. Yet another process disclosed in this patent is one referred to therein as a "one-step" process. This one-step process involves preparing a mixture of the polyalkene and the maleic reactant containing the necessary amounts of both to provide the desired substituted succinic acylating agents, i.e., at least 1.3 moles of maleic reactant for each mole of polyalkene in order that there can be at least 1.3 succinic groups for each equivalent weight of substituent groups. Chlorine is then introduced into the mixture, usually by passing chlorine gas through the mixture with agitation, while maintaining a temperature of at least about 140C. A variation on this process involves adding additional maleic reactants during or subsequent to the chlorine introduction. Chlorine may be introduced continuously or intermittently during the one-step process. The rate of introduction of the chlorine is not critical although, for maximum utilization of the chlorine, the rate should be about the same as the rate of consumption of chlorine in the course of the reaction.
When the introduction rate of chlorine exceeds the rate of consumption, chlorine is evolved from the reaction mixture. The minimum temperature at which the reaction in the one-step process takes place at a reasonable rate is about 140C. Thus, the minimum temperature at which the process i8 normally carried out is in the neighborhood of 140C. The preferred temperature range is usually between about 160-C and about 220-C. Higher temperatures such as 250-C or even higher may be used but usually with little advantage. In the one-step process, the molar ratio of maleic reactant to chlorine is such that there is at least about one mole of chlorine for each mole of maleic reactant to be incorporated into the product. Moreover, for practical reasons, a slight excess, usually in the neighborhood of about 5% to about 30% by weight of chlorine, is utilized in order to offset any loss of chlorine from the reaction mixture. Larger amounts of excess chlorine may be used but do not appear to produce any beneficial results.
International Patent Application Number W0 85/03,S04 discloses an improvement in known processes for preparing substituted-carboxylic acids useful as acylating agents which comprise the reaction of (A) at least one aliphatic polymer of one or more lower olefins with (B) an acid reactant selected from the group consisting of fumaric acid, itaconic acid, maleic acid, and the corresponding anhydrides, lower alkyl esters, acyl chlorides and acyl bromides, in the presence of chlorine can be improved by the steps of (i) reacting at a temperature of about lO0-200 C, a mixture of (A) and (B) in the presence of about 0.05 to 0.15 equivalent of chlorine per equivalent of (A) until the chlorine has reacted to provide a first intermediate product, (ii) continuing the reaction in the absence of chlorine at a temperature of from about 180-250C until a conversion of 0.4 to 1.1 equivalents of (B) per equivalent of (A) is attained to provide a second intermediate product, and (iii) reacting said intermediate with about 0.2 to 1.5 equivalents of chlorine per equivalent o~f (A) used in step (i) at a temperature of about 180-225C.

The processes described in these patents suffer -from one or more of the following drawbacks: the presence of relatively large amounts of unfunctionalized hydrocarbon polymer in the product residue, which unfunctionalized hydrocarbon polymer is very difficult or even impossible to efficiently and economically remove from the product residue; the presence in the product residue of insoluble sediment formed by more than one maleic anhydride group being incorporated into a single molecule of hydrocarbon polymer thereby reducing the proportion of hydrocarbon polymer available to maintain oil solubility; and the presen¢e in the product residue of oxidized material which has been generated from the hydrocarbon polymer reactant or from the long chain hydrocarbyl substituted dicarboxylic acid material product, due to the harsh conditions of the oxidative and high temperature reaction environment.
It is apparent, therefore, that there is a need for a process which eliminates or reduces the drawbacks suffered by these prior processes, particularly in the use of high molecular weight polymers. The present invention provides such a process.
It is known from James V. Oldshue, Fluid Mixing Technoloqy, p. 178 (McGraw Hill 1983), that as the ratio of tank depth-to-diameter increases, the use of multiple impellers is often recommended to improve the top-to-bottom flow over that which can be maintained (with difficulty) by use of a single axial-flow impeller. It is taught therein that inclusion of a second impeller does not have a significant impact on pumping volume. Rather, its principal purpose is to maintain a full top-to-bottom flow pattern, thereby utilizing the full depth of the tank.

- lo- 133~895 SUMMARY OF THE lN V~N~ oN

In accordance with the instant invention there is provided a process for the preparation of long chain hydroaarbyl substituted mono- or dicarboxylic acid materials which comprises contacting in a reaction zone (provided with plural zone mixing as hereinafter defined) a long chain hydrocarbon polymer, generally a polyolefin, and an ethylenically unsaturated mono- or dicarboxylic acid material such as maleic anhydride~with chlorine, with at least about 60 mol% of said chlorine being added to the reaction mixture containing said polyolefin and ethylenically unsaturated mono- or dicarboxylic acid material at a reaction temperature below about 170-C., wherein the reaction mixture is mixed employing a mixing energy of at least 4 HP/1000 gal. at least during the contacting of the chlorine therewith.
This process produces relatively high conversions of hydrocarbon polymer reactant to long chain hydrocarbyl substituted mono- or dicarboxylic acid material product, thereby reducing the amount of unfunctionalized hydrocarbon polymer in the product residue or mixture. This process selectivity produces more monofunctionalized long chain hydrocarbyl substituted mono- or dicarboxylic acid material product, i.e., wherein one molecule of long chain hydrocarbon polymer has one molecule of a mono- or dicarboxylic acid material attached thereto, for any given degree of incorporation of the mono- or dicarboxylic acid material, thereby enhancing the oil solubility of the product residue or mixture, and substantially reduces the amount of oxidized material generated from the hydrocarbon polymer reactant or from the mono- or dicarboxylic~-acid material functionalized hydrocarbon polymer product. The proces~ of this invention can therefore also provide products of improved, low color which con-tain decreased . ~. .

amounts of undesired reaction by-products. Further, the process of this invention provides improved polymer conversion efficiencies. Still further, the process can provide substantially complete chlorine utilization and minimizes or avoids chlorine gas breakthrough, thereby minimizing the C12 gas loss and the at~en~Ant equipment and materials cost associated with treatment of substantial C12 content gases in any overhead gas condenser/liquid recycle or other gas effluent system (e.g. gas scrubbers).

BRIEF DISCRIPTION OF THE ACCOMPANYING DRAWINGS

Figure 1 is a cross-sectional diagrammatical view of a reaction zone useful in one embodiment of the process of the present invention employing dual zone mixing.
Figure 2 is a graphical plot of mixing power numbers (Np) versus mixing Reynolds Numbers (NRe) for a series of curves 1 through 7 providing correlations for the indicated types of impellers. Curves 1 and 3 apply to disk flat blade turbines, curves 2 and 4 to vertical fixed blade turbines, curve 5 to curved blade turbines, curve 6 to 45-pitched blade turbines and curve 7 to retreat blade turbines, in full baffled stirred tank reactors, wherein the impeller blades are characterized by the indicated ratio of the blade's diameter "D" to the vertical-component width "wn.
DESCRIPTION OF THE lNV~I. llON

In accordance with the present invention there is provided a process for the preparation of long chain hydro-carbyl substituted mono- or dicarboxylic acid material produat. The process of the instant invention comprises intimately contacting a reaction mixture comprising (A) long chain hydrocarbon polymer, generally a polyolefin, and (B) ethylenically unsaturated mono- or dicarboxylic acid material with chlorine, with about 70 to 100%, preferably to 100%, and more preferably about 90 to 100%, of the total amount of chlorine employed in the process being added to said reaction mixture at a reaction temperature of not greater than about 170-C., wherein the reaction mixture is ~ixed at high total mixing energies, as defined hereinafter.
The long chain hydrocarbyl substituted mono- or dicarboxylic acid material includes the reaction products of the long chain hydrocarbon polymer, generally a polyolefin, with the monounsaturated carboxylic reactant comprising at least one member selected from the group consisting f (i) monounsaturated c4 to C10 dicarboxylic acid wherein (a) the carboxyl groups are preferably vicinal, (i.e. located on adjacent carbon atoms) and (b) at least one, preferably both, of said adjacent carbon atoms are part of said mono unsaturation; (ii) derivatives of (i) such as anhydrides or Cl to C5 alcohol derived mono- or di-esters of (i); (iii) monounsaturated C3 to C10 monocarboxylic acid wherein the carbon-carbon double bond is conjugated to the carboxy group, i.e, of the structure o --C=C--C-- ;
and (iv) derivatives of (iii) such as Cl to C5 alcohol derived monoesters of (iii). Upon reaction with the polymer, the monounsaturation of the monounsaturated carboxylic reactant becomes saturated. Thus, for example, maleic anhydride becomes a polymer substituted succinic anhydride, and acrylic acid becomes a polymer substituted propionic acid.
Normally, not all of the polyolefin reacts with the unsaturated mono- or dicarboxylic acid material, i.e., acid or derivative, and the hydrocarbyl substituted mono-or dicarboxylic acid material will contain non-acid substituted polyolefin. The hydrocarbyl substituted mono-or dicarboxylic acid material (also referred to herein as "functionalized~ polymer or polyolefin), non-acid substituted polyolefin, and any other polymeric byproducts, e.g. chlorinated polyolefin, (also referred to herein as ~unfunctionalized" polymer~ are collectively referred to herein as "product residue" or ~product mixture". The non-acid substituted polyolefin is typically not removed from the product mixture because such removal is difficult and would be commercially unfeasible, and the product mixture, stripped of any unreacted monounsaturated C4 to C10 mono- or dicarboxylic acid, anhydride, or ester is employed per se as a lubricating or fuel oil additive or as an intermediate for further reaction with, inter alia, polyfunctional materials such as polyols or polyamines to form additives such as dispersants for lubricating oils or-fuel oils.
One of the principal advantages of the instant process over the prior art processes resides in minimizing the amount of this unfunctionalized polyolefin present in the product mixture. This is due to the fact that by the use of the instant process relatively high conversions of the polyolefin reactant, on the order of at least about 80%, preferably at least about 85% (e.g. 85 to 100%), and more preferably from about 8S to 95% of the long chain hydrocarbyl substituted carboxylic acid material obtained, thereby minimizing the amount of unfunctionalized polyolefin in the product mixture.
The reaction of the hydrocarbon polymer, e.g., polyolefin, with the unsaturated mono- or dicarboxylic acid material generally produces more than one species of long chain hydrocarbyl substituted mono- or dicarboxylic acid material. One species, referred to herein as monofunctional long chain hydrocarbyl substituted mono- or dicarboxylic acid material, comprises a polyolefin molecule - 14 - 1 3 3~ 8g S

having only one mono- or dicarboxylic acid material moiety attached thereto. Such a monofunctional species is produced when only one molecule of unsaturated mono- or dicarboxylic acid material reacts with one molecule of polyolefin. Another species, referred to herein as polyfunctional long chain hydrocarbyl substituted acid material, comprises a polyolefin molecule having more than one, usually two, mono- or dicarboxylic acid material moieties attached thereto. Such a polyfunctional species is produced when more than one, usually two, molecules of unsaturated mono- or dicarboxylic acid material react with the same molecule of polyolefin.
Another advantage of the present process is that it is surprisingly selective for the monofunctional species, i.e., the monofunctional long chain hydrocarbyl substituted mono- or dicarboxylic acid material is produced in preference to the polyfunctional long chain hydrocarbyl substituted mono- or dicarboxylic acid material. It is to be understood that this selectivity is not exclusive and some of the polyfunctional species may also be produced.
However, the proportion of the monofunctional species produced to the polyfunctional species produced is substantially higher than in conventional prior art process utilizing higher reaction temperatures.
Moreover, it has been surprisingly found that the process of this invention permits the formation of such high proportions of monofunctional species simultaneously with the high conversions to total substituted species.
This process, therefore, has been surprisingly found to maximize both total conversion to product and the selectivity to monofunctional long chain hydrocarbyl substituted mono- or dicarboxylic acid material. As a consequence, high polymer conversion efficiencies (as hereinafter defined) can be achieved.

- 15 - 133~895 Yet another advantage of the instant process is improved low color and the reduction in the amount of oxidized material produced. This oxidized material is generally generated from the polyolefin reactant or from the long chain hydrocarbyl substituted mono- or dicarboxylic acid material due to the harsh conditions of the oxidative and high temperature reaction environment.
The utilization of lower temperatures in the instant process reduces the amounts of these oxidized materials which are formed during the reaction.
Further, the process of this invention has been found to achieve some or all of the above advantages with greatly reduced levels of sediment formation in the reaction. Such sediment is highly undesirable on an industrial scale, since it contributes substantial cost to the manufacturing process due to the need to remove and dispose of this undesired by-product.
Exemplary of such monounsaturated carboxylic reactants are fumaric acid, itaconic acid, maleic acid, malei¢ anhydride, chloromaleic acid, chloromaleic anhydride, acrylic acid, methacrylic acid, crotonic acid, cinnamic acid, and lower alkyl (e.g., Cl to C4 alkyl) acid esters of the foregoing, e.g., methyl maleate, ethyl fumarate, methyl fumarate, etc.
The olefin polymers for reaction with the unsaturated mono- or dicarboxylic acid material are homopolymers and interpolymers of polymerizable olefin monomers of 2 to about 16 carbon atoms, usually 2 to about carbon atoms. The interpolymers are those in which two or more olefin monomers are interpolymerized according to well-known conventional procedures to form polyolefins having units within their structure derived from each of said two or more olefin monomers. Thus, "interpolymer(s)"
as used herein is inclusive of copolymers, terpolymers, tetrapolymers, and the like. As will be apparent to those of ordinary skill in the art, these polyolefins are often conventionally referred to as "polyalkenes".
The olefin monomers from which the polyolefins are derived are polymerizable olefin monomers characterized by the presence of one or more ethylenically unsaturated yLOU~3 (i.e., > C = C <); that is, they are mono-olefinic monomers such as ethylene, propylene, butene-l, isobutene, and octene-l or polyolefinic monomers (usually diolefinic monomers) such as butadiene-1,3 and isoprene.
These olefin monomers are usually polymerizable terminal olefins; that is, olefins characterized by the presence in their structure of the group > C = CH2.
However, polymerizable internal olefin monomers (sometimes referred to in the patent literature as medial olefins) characterized by the presence within their structure of the group > C -- C = C -- C <

can also be used to form the polyolefins. When internal olefin monomers are employed, they normally will be employed with terminal olefins to produce polyolefins which are interpolymers. For purposes of this invention, when a particular polymerized olefin monomer can be classified as both a terminal olefin and an internal olefin, it will be deemed to be a terminal olefin. Thus, pentadiene-1,3 (i.e.
piperylene) is deemed to be a terminal olefin for purposes of this invention.
While the polyolefins generally are hydrocarbon polyolefins, they can contain non-hydrocarbon groups such as lower alkoxy, lower alkyl mercapto, hydroxy, mercapto, carboxy, (i.e., -- C --as in keto and aldehydo ~Lou~S), nitro, halo, cyano, carboalkoxy (i.e., > C - 0 - alkyl where "alkyl" is usually lower alkyl); alkanoyloxy where alkyl is usually lower alkyl, and the like provided the non-hydrocarbon substituents do not substantially interfere with formation of the long chain hydrocarbyl substituted mono- or dicarboxylic acid materials of this invention.
When present, such non-hydrocarbon groups normally will not contribute more than about 10% by weight of the total weight of the polyolefins. Since the polyolefin can contain such non-hydrocarbon substituent, it is apparent that the olefin monomers from which the polyolefins are made can also contain such substituents. Normally, however, as a matter of practicality and expense, the olefin monomers and the polyolefins will be free from non-hydrocarbon groups.
Although the polyolefins may include aromatic groups (especially phenyl groups and lower alkyl- and/or lower alkoxy-substituted phenyl groups such as para-(tertbutyl) phenyl) and cycloaliphatic groups such as would be obtained from polymerizable cyclic olefins or cycloaliphatic substituted polymerizable acyclic olefins, the polyolefins usually will be free from such groups.
Nevertheless, polyolefins derived from interpolymers of both 1,3-dienes and styrenes such as butadiene-1,3 and styrene or para-(tert-butyl)styrene are exceptions to this generalization. Again, because aromatic and cycloaliphatic groups can be present, the olefin monomers from which the polyolefins are prepared can contain aromatic and cycloaliphatic groups.
From what has been described hereinabove in regard to the polyolefin, it is clear that there is a general preference for aliphatic, hydrocarbon polyolefins free from aromatic and cycloaliphatic groups (other than the diene styrene interpolymer exception already noted). Within this general preference, there is a further preference for polyolefins which are derived from the group consisting of homopolymers and interpolymers of terminal hydrocarbon olefins of 2 to about 16 carbon atoms. This further preference is qualified by the proviso that, while interpolymers of terminal olefins are usually preferred, interpolymers optionally containing up to about 40% of polymer units derived from internal olefins of up to about 16 carbon atoms are also within a preferred group. A more preferred class of polyolefins are those selected from the group consisting of homopolymers and interpolymers of terminal olefins of 2 to about 6 carbon atoms, more preferably 2 to 4 carbon atoms, optionally containing up to about 25% of polymer units derived from internal olefins of up to about 6 carbon atoms.
Specific examples of terminal and internal olefin monomers which can be used to prepare the polyolefins according to conventional, well-known polymerization tec-hn;ques include ethylene; propylene; butene-l; butene-2;
isobutene; pentene-1; hexene-1; heptene-1; octene-1;
nonene-1; decene-1; pentene-2; propylene-tetramer;
diisobutylene; isobutylene trimer; butadiene-1,2;
butadiene-1,3; pentadiene-1,2;pentadiene-1,3;
pentadiene-1,4; isoprene;hexadiene-1,5;
2-chloro-butadiene-1,3; 2-methyl-heptene-1;

3-cyclohexylbutene-1; 2-methyl-5-propyl-hexene-1;
pentene-3; octene-4; 3,3-dimethyl-pentene-1; styrene;
2,4-dichloro styrene; divinylbenzene; vinyl acetate; allyl alcohol; l-methyl-vinyl acetate; acrylonnitrile; ethyl acrylate; methyl methacrylate; ethyl vinyl ether; and methyl vinyl ketone. Of these, the hydrocarbon polymerizable monomers are preferred and of these hydroaarbon monomers, the terminal olefin monomers are particularly preferred.

Specific examples of polyolefins include polypropylenes, polybutenes, ethylene-propylene copolymers, styrene-isobutene copolymers, isobutene-butadiene-1,3 copolymers, propene-isoprene copolymers, isobutene-chloroprene copolymers, isobutene-(para methyl)styrene copolymers, copolymers of hexene-l with hexadiene-1,3, copolymers of octene-l with hexene-1, copolymers of heptene-l with pentene-l, copolymers of 3-methyl-butene-1 with octene-1, copolymers of 3,3-dimethyl-pentene-1 with hexene-l, and terpolymers of isobutene, styrene and piperylene. More specific examples of such interpolymers include copolymer of 95% (by weight) of isobutene with 5% (by weight) of styrene; terpolymer of 98% of isobutene with 1% of piperylene and 1% of chloroprene; terpolymer of 95% of isobutene with 2% of butene-l and 3% of hexene-l; terpolymer of 60% of isobutene with 20% of pentene-l and 20% of octene-l; copolymer of 80%
of hexene-l and 20% of heptene-1; terpolymer of 90% of isobutene with 2% of cyclohexene and 8% of propylene; and copolymer of 80% of ethylene and 20% of propylene. A
preferred source of polyolefins are the poly(isobutene)s obtained by polymerization of C4 refinery stream having a butene content of about 35 to about 75 percent by weight and an isobutene content of about 30 to about 60 percent by weight in the presence of a Lewis acid catalysts such as aluminum trichloride or boron trifluoride. These polybutenes contain predominantly (greater than about 80%
of the total repeating units) of isobutene repeating units of the configuration CH2 Cl -- 133589~

In some cases, the olefin polymer may be completely saturated, for example an ethylene-propylene copolymer made by a Ziegler-Natta synthesis using hydrogen as a moderator to control molecular weight.
The polyolefins used in the instant process generally have number average molecular weights (~n) f at least about 1,200, e.g., within the range of about 1,200 to about 5,000, preferably at least about 1,500, e.g., between about 1,500 and about 5,000, more preferably at least about 1,900, e.g., between about 1,900 and about 4,000, and most preferably at least about 2,200, e.g., between about 2,200 and 4,000. The number average molecular weight for such polymers can be determined by several known te~hniques. A convenient method for such determination is by gel permeation chromatography (GPC) which additionally provides molecular weight distribution information, see W. W. Yau, J. J.
Kirkland and D. D. Bly, "Modern Size Exclusion Liquid Chromatography", John Wiley and Sons, New York, 1979. The olefin polymers will generally have (or can be treated, e.g. by fractionation, to form) a molecular weight distribution ~w/~n (that is, the ratio of the weight average molecular weight to the number average molecular weight) of from about 1.0 to 4.5, and more typically from about 1.5 to 3Ø
In the instant process typically at least about 0.5 (e.g. from about 0.5 to about 1.5), preferably from about 0.7 to about 1.4, and more preferably from about 1.0 to about 1.3, moles of unsaturated mono- or dicarboxylic acid material reactant are charged to the reactor per mole of polyolefin reactant to form an initial reaction mixture into which chlorine is introduced under controlled reaction temperature conditions. It is generally preferred to utilize amounts of unsaturated mono- or dicarboxylic acid material reactant which facilitate the selectivity of the - 21 - 1~S895 instant process for the monofunctional species of the long chain hydrocarbyl substituted mono- or dicarboxylic acid material product. This initial reaction mixture may or may not contain the total amount of the unsaturated mono- or dicarboxylic acid material reactant which is charged to the reactor. If it does not contain all of the unsaturated mono- or dicarboxylic acid material reactant~the remainder of the acid material reactant is added to the reaction mixture simultaneously with or after the introduction of chlorine has begun, with all of the remainder of said acid material being added to the reaction mixture before the introduction of the chlorine is terminated. In the case where the initial reaction mixture does not contain all of the unsaturated mono- or dicarboxylic acid material reactant it contains at least sufficient acid material reactant to minimize degradation of the polyolefin reactant by the chlorine.
Preferably the initial reaction mixture, prior to the introduction of the chlorine, contains at least about mole % of the total unsaturated mono- or dicarboxylic acid material reactant charged to the reactor. More preferably the initial reaction mixture contains 100 mole %
of the total unsaturated mono- or dicarboxylic acid material reactant charged to the reactor by the time that an amount of chlorine constituting about 20 - 40 mole % of the total chlorine (C12) charge is introduced into the initial reaction mixture.
If the initial reaction mixture does not contain all of the unsaturated mono- or dicarboxylic acid material reactant prior to the introduction of chlorine the remainder of the acid reactant charge may be charged into the initial reaction mixture continuously or intermittently and concurrently with the start of chlorine introduction or after the introduction of chlorine has begun. Furthermore, it may be charged simultaneously with the chlorine, or - 22 - 13 3 589~

sequentially with the chlorine, e.g., discrete charge of acid material followed by and alternating with a discrete charge of chlorine, provided the total acid material charge is charged into the reaction mixture before the total chlorine charge is charged into the reaction mixture.
The total amount of chlorine charge introduced into the reaction mixture, i.e., the total amount of chlorine employed in the process, is generally at least about 0.6, e.g., from about 0.6 to about 1.5, preferably at least about 0.8, e.g., from about 0.8 to about 1.3, more preferably greater than 0.95, e.g., 0.95 to about 1.25, and most preferably at least about 1.01, e.g., about 1.05 to 1.2, moles of chlorine per mole of the total charge of unsaturated mono- or dicarboxylic acid material reactant.
Generally, a mole ratio of chlorine to unsaturated mono- or dicarboxylic acid of about 1.5:1, preferably about 1.3:1, more preferably about 1.2:1, and most preferably about 1.1:1, should not be exceeded. It is most preferred to use at least equimolar amounts of chlorine, i.e., equimolar ~r a minor excess.
In various embodiments of the present invention the ahlorine can be introduced in different manners. For example, in a certain embodiment the chlorine is introduced continuously or intermittently over a period of time. As mentioned hereinafore the chlorine may be introduced into the initial reaction mixture containing the total or partial unsaturated mono- or dicarboxylic acid material reactant charge. In the latter case the chlorine may be introduced simultaneously with the remaining uncharged unsaturated mono- or dicarboxylic acid material or in alternating charges of chlorine and unsaturated mono- or dicarboxylic acid material.
In one embodiment the initial reaction mixture contains the total unsaturated mono- or dicarboxylic acid material charge (admixed with the total polyolefin charge) 133~89~

and chlorine is charged into the reaction mixture in a continuous manner. In another embodiment chlorine is charged intermittently into a reaction mixture containing the total unsaturated mono- or dicarboxylic acid material and polyolefin charges.
In still another embodiment into an initial reaction mixture containing 100 mole % of the total polyolefin charge and about 50 mole % of the total unsaturated mono- or dicarboxylic acid material charge there are introduced, simultaneously, chlorine and unsaturated mono- or dicarboxylic acid material. The relative rate of introduction of chlorine and remaining uncharged acid material is such that when the reaction mixture contains 100 mole % of the acid material charged it contains about 30 mole % of the total chlorine charge, i.e., during this period about 50 mole % of the total charge of acid material and about 30 mole % of the total chlorine charge are introduced. The remaining 70 mole % of the total chlorine charge is then introduced into the reaction mixture.
The upper reaction temperature limit at which the majority of the chlorine is introduced in the instant proce$s is critical. Thus, it is critical that at least about 60 mole %, preferably at least about 70 mole %, more preferably at least 90 mole %, and most preferably 100 mole % of the total chlorine charge be introduced into and intimately contacted with the reaction mixture at a reaction temperature of not greater than about 170C.
After the above chlorine charges are effected, the reaction mixture's temperature can be raised above 170C., preferably between about 170- to 200C, during the introduction of the remaining chlorine charge. The reaction mixture is then maintained at this further elevated temperature until the reaction is complete, i.e., until the evolution of hydrogen chloride ceases or until the desired degree of reaction is obtained.

- 24 - 13358g5 The lower temperature limit during the introduction of chlorine and at which the reaction is carried out should be effective to form the long chain hydrocarbyl substituted mono- or dicarboxylic acid material. Generally such temperatures should not fall below about 60-C. preferably not below about lOO-C., and most preferably not below about llO-C.
Thus, for example, in the case where 100 mol % of the chlorine charge is introduced into the initial reaction mixtu*e at a temperature not greater than about 170-C. the reaction mixture is preferably maintained, during and subsequent to the chlorine introduction, at temperatures in the range of from about lOO-C to 170-C. In the two stage chlorine addition embodiment wherein at least about 60 mol ~ of the total chlorine charge is first introduced into the initial reaction mixture at a temperature not greater than about 170-C. followed by the remainder of the total chlorine charge being added at a temperature above about 170-C., the temperature during the introduction of this first charge of chlorine is generally in the range of about 110C. to 170-C., and is subsequently raised during the introduction of the remainder of the chlorine charge to from about 170-C. to 200-C.
Preferably, in addition to observing the above critical chlorine charge temperatures at least about 20 mol %, and more preferably at least about 25 mol %, of the total chlorine charge is introduced into and intimately contacted with the reaction mixture at a reaction temperature of not greater than about 150-C.
If desired, a catalyst or promoter for reaction of the olefin polymer and monounsaturated carboxylic reactant (whether the olefin polymer and monounsaturated carboxylic reactant are contacted in the presence or absence of halogen (e.g., chlorine)) can be employed in the reaction zone. Such catalyst of promoters include alkoxides of Ti, - ` 133~895 Zr, V and Al, and nickel salts (e.g., Ni acetoacetonate and Ni iodide) which catalysts or promoters will be generally - employed in an amount of from about 1 to S,000 ppm by weight, based on the mass of the reaction medium.
- The reaction times of the process are times which are effective for the reaction process will generally be dependent, at least to a degree, upon such variables as volume of the reaction mass, the temperature and concentration of the reactants, and other factors.
Generally, however, the reaction time of the process ranges from about 0.5 hour to about 15 hours, and more usually from about 3 to about 10 hours. As is apparent to those skilled in the art, the duration of the reaction will depend at least in part on such variables as the quantity of reactants, reaction temperature, and the like.
The process of this invention can be carried out in the presence of a substantially inert, normally liquid solvent/diluent such as hydrocarbon mineral oils of lubricating oil viscosity, lower molecular weight hydrocarbon solvents. However, solvents generally are not necessary and in a preferred embodiment as described hereinafter are not used. When volatile lower molecular weight hydrocarbon solvents are used, it is often preferred to carry out the reaction at pressures in excess of atmospheric. Generally, however, the reaction can be carried out at atmospheric pressure or at pressures ranging up to about five atmospheres.
Since it is critical that the temperature of the reaction mixture be below about 170C. throughout the entire chlorine addition period in one embodiment of the invention) and throughout the period of introduction of at least 60 mole % of the total amount of chlorine added to the reaction mixture in the second embodiment of the invention, and since the reaction is exothermic, it is necessary to take steps to keep the temperature of the reaction mixture at or below this critical upper limit.
This can be accomplished by controlling the rate of chlorine addition, by cooling the reactor vessel, or both.
Generally, the slower the rate of chlorine introduction into the reaction mixture the lower the temperature of the reaction mixture. Thus, the rate of chlorine addition should be such as to keep the temperature of the reaction mixture below about 170-C. Such rate can be varied over time as needed to assist in such temperature control.
However, in some cases controlling the temperature by controlling the rate of chlorine addition alone may be impossible or impractical. In such cases cooling of the reactor vessel, either in combination with adjusting the rate of chlorine addition or alone may be employed.
In the embodiment wherein a portion of the total chlorine charge is added to the reaction mixture maintained at a temperature below about 170C., and the remainder of the chlorine charge is then added to the reaction mixture at temperatures above 170C., it may sometimes be necessary or desirable to heat the reactor to achieve and maintain these elevated temperatures. However, in some situations the temperature of the reaction mixture can be maintained above about 170C. by merely regulating, e.g., increasing, the rate of chlorine addition. In such cases heating the reactor to obtain these elevated temperatures is not nec~cs -ry .
While the reaction can be carried out in the presence of air, the reaction is preferably carried out under an inert environment, e.g., in an inert atmosphere such as by nitrogen blanketing. The inert environment, which is preferred, should be free of oxygen.
Conducting the instant process at the critical relatively low temperatures causes the viscosity of the reaction mixture to increase, making it more difficult for the polyolefin/unsaturated mono- or dicarboxylic acid material reactant mixture to be homogeneous. It also becomes more difficult for the chlorine, generally introduced into the reaction mixture as a gas, to react uniformly with the viscous polymer leading to localized pockets of reaction which counteract the advantageous effects, described hereinbefore, of the instant process.
Hence, a high total mixing energy is required to be able to obtain the benefits, particularly high conversion of the polyolefin, of the instant process. Therefore, the instant invention requires the introduction of chlorine gas, preferably into the lower portion of the liquid, initial reaction mixture containing polyolefin reactant and monounsaturated carboxylic reactant, while mixing or stirring the initial reaction mixture for a time and under conditions sufficient to provide substantial homogeneity of the reaction mixture and substantial chlorine gas dispersion throughout the reaction mixture. Such mixing should impart a total mixing energy to the liquid reaction mixture of at least about 4 HP (horsepower)/1000 gal.
(e.g., in the range of from about 5 to 30 HP/1000 gal.), preferably at least about 10 HP/1000 gal., and more preferably in the range of from about 10 to 30 HP/1000 gal.
and most preferably from about 10 to 20 HP/1000 gal. The "total mixing energy" is herein intended to refer to the sum of the mixing energy imparted to the liquid reaction mixture by each mixing means, that is impeller, gas or liquid sparger, fluid impact sparger, etc., used.
Mixing force can be imparted to the reaction mixture in each mixing zone by one or more mixing means, including ultrasonic mixers, impellers, gas spargers, liquid injectors, or fluid impact spargers. Gas sparging can employ chlorine gas and/or an inert gas (e.g. N2).
Liquid injectors can employ an inert liquid and/or one of the liquid reactants. Impact sparging can be accomplished by withdrawing a portion of the reaction liquid (e.g., from -i - 28 - 13~895 the Upper portion of the reaction zone) and reintroducing the liquid via one or more injectors or nozzles into the reaction zone (e.g., into the lower portion of the reaction zone), together with gaseous chlorine, which can be admixed with the reintroduced liquid prior to, in or immediately after the injectors or nozzles, thereby subjecting the gas to high shear conditions imparted by the high liquid velocities and providing high mixing energies to the reaction mixture.
Preferably, the mixing energy to the reaction mixture in at least one mixing zone is provided by at least one impeller. For convenience, the "mixing energy"
imparted to reaction liquids by impellers is herein intended to refer to the energy imparted to the liquid reaction mixture under no-gas conditions, that is in the absence of gas introduced.
Mixing energies (in units of horsepower per thousand gallons), can be determined for a given mixing device by conventional means, and for each impeller can be calcu}ated from the equation:
Pw (HP/l,000 gal.) = (I) V

wherein "V" is the volume of the reaction liquid (in units of thousands of U.S. gallons) and ~Pw~ represents the power consumed by the impeller in units of horsepower and is calculated from the equation:

P = (2.62 X 10 ) (N ) (p ) (N ) (D ) (II) w p wherein "Np" is the power number for the impeller employed, " ~ " is the liquid's density (at 120C, in units of pounds per cubic foot), "Ni" is the impeller rotation speed under no-gas conditions (in units of revolutions per ~ - 29 - 1335895 minute), ~Di" is the impeller diameter (in units of feet), and 2.62 x lo~10 is the conversion factor for these units.
The power number "Np" for a given impeller in the reaction liquids of the present invention can be determined by conventional means. For example, the Nagata correlation (Shinji Nagata, Mixing-Principles and Applications, p. 32, Equation 1.50 (Halsted Press, N.Y., 1975)) can be employed for an unbaf~led reactor, given the dimensions of the impeller, the density and viscosity of the particular reaction liquid employed and other factors. For commerical impellers, standard correlations (e.g. curves) exist from which "Np" values can be derived, given the particular impeller used and the dimensionless Mixing Reynolds Number "NRe" of the reactor, which can be determined from the equation:

(~ ) (Ni)(Di)2 NRe = 24.8 (~II) ~ ) wherein " ~ ", "Ni" and "Di" are as defined above, ~ "
is the liquid viscosity (at 120C, in units of centipoise), and 24.8 is the conversion factor for these units.
For example, "Np values can be calculated for stirred tank reactors as described in D. S. Dickey et al., "Dimensional Analysis for Fluid Agitation Systems", Chemical Engineerinq, pages 139-145 (January 5, 197~), and in James Y. Oldshue, Fluid Mixing Technology (McGraw Hill 1983), see e.g. pp 43-71, Chapter 3, "Power Correlations and the Effects of Mixing Environment". Figure 2 hereof also ~rovides N v NRe correlations for baffled stirred tank reactors employing any of the impell~rs identified for~curves 1 to 7 -133589~

For the purposes of this invention, "Np"
determinations are made assuming each impeller is immersed in the liquid and further assuming a single phase liquid, under no-gas conditions, that is using the NRe and any liquid property parameters (viscosity and density at 120C) calculated on the assumption that the liquid contains only the high molecular polymer (e.g., polyisobutylene) to be charged for the reaction.
The degree of mixing in commerical stirred tank reactors can be increased by use of conventional baffles along the reactor walls, generally from 1 to 6 baffles, more usually from 3 to 5 baffles, (e.g. vertical or inclined (15 to 30) flat plate baffles, vertical cylinders, etc.) each having a width of from about 2 to 15%
of the inner tank diameter. Baffles generally will be spaced at equal distances about the tank's circumference (e.g. 4 baffles spaced 90 apart) and can be positioned with a clearance (e.g., of a distance equal to from about 5 to 40% of the baffle's width) from the reactor's side wall.
In accordance with the process of this invention, the initial liquid reaction mixture, comprising the liquid polyolefin and monounsaturated carboxylic reactant charge, is contacted at high total mixing energies in a reaction zone provided with plural zone mixing comprising at least one high shear zone, adapted for dispersion of gas bubbles in the liquid reaction mixture, and at least one axial gas pumping zone, adapted for recirculation of gas bubbles axially in the liquid reaction mixture, whereby the chlorine gas is introduced into the liquid reaction mixture in the high shear zone. Preferably, the axial gas pumping zone comprises a downwardly gas pumping zone and is most preferably located above the high shear zone.
The process of this invention is particularly suited for, and its observable benefits are notably pronounced in, large reactors (e.g., commercial scale - 31 - 133~895 stirred tank reactors), as contrasted to small reactor vessels (e.g., pilot or laboratory scale equipment), wherein wall-effects and other small-scale equipment effects, can mask the surprising benefits which have been found in use of the plural zone high mixing, low temperature chlorination process of the present invention.
Therefore, the liquid reaction mixture of the present invention will comprise at least about 70 Kg, and preferably at least about 100 Kg, calculated on the basis of the long chain hydrocarbon polymer charged to the reaction zone.
Reference is now made to Figure 1 wherein the same numbers refer to the same or similar elements. In Figure 1, one embodiment of the preferred reaction zones for effecting the process of this invention is illustrated, comprising a stirred tank reaction vessel 10 (having inside diameter ~Dr) provided with internal side walls 12, a plurality (e.g. 3 to 5) of flat plate baffles 70 affixed to side walls 12, internal bottom surface 14, upper closure member 16 and upper closure member inner surface 15, defining reaction zone 20. Reactor 10 is provided with a high shear impeller means 45 (which in the embodiment illustrated comprises a disk fixed blade turbine (having 6 blades 44), and an axial pumping impeller means 43 (which in the illustrated embodiment comprises a downwardly pumping impeller having 6 45-pitched blades 42) which are rotatably affixed to a center shaft 40, positioned substantially along the vertical center axis 41 of reactor 10. Reactor 10 is provided with a polymer supply conduit 19 for feed of the polymer reactant, and reaction diluent or solvent, if employed, into the reaction zone 20, and with a product mixture withdrawal conduit 18 for withdrawing liquid reaction mixture from reactor 10.
Reactor 10 is also provided with monounsaturated carboxylic reactant injection means comprising a conduit - 32 - 133~895 30, and with chlorine injection means, comprising conduit 50. Chlorine injection means 50 preferably is adapted to introduce gaseous chlorine into liquid reaction medium 20 below lower high shear impeller means 45. Preferably, carboxylic reactant introduction means 30 is adapted to introduce monounsaturated carboxylic reactant into reactor 10 above upper impeller means 43.
Conduits 50, 30, 19 and 18 are provided with conventional valve means for controlling the rate of the respective gas and liquid feeds and withdrawals. Reactor can also be provided with an overhead vapor withdrawal conduit (not shown) for withdrawal of vapors from reactor to an external condenser for partial or complete condensation of these vapors. A liquid recycle of a portion of such condensate as reflux to reaction zone 20 (via a reflux conduit, not shown) can be employed, if desired, for reaction liquid level and temperature control and to maximize utilization of the monounsatured carboxylic reactant.
The high shear impeller means 45 will generally comprise a dispersing turbine, and can employ flat blades or pitched blades (generally from 2 to 8 blades per impeller). Where pitched blades are employed, high shear impeller 45 will additionally perform either a downward or upward pumping (i.e. "axial" pumping) function, depending on the positioning of the pitch relative to the vertical and the direction in which the turbine is turned. High shear impeller means 45 preferably comprises a plurality of impeller blades 44 (six blades in the illustrated embodiment), which are substantially vertically positioned.
Axial pumping impeller means 43 can comprise a pitched blade or a propeller turbine, wherein such pitched blades can either be fixed or adjustable and wherein the angle of pitch can be constant or varied along the length of one or more such blades (e.g., as in a variable curve retreat curve blade turbine) or a draft tube circulator.
Axial pumping impeller 43 will generally comprise from 3 to 8 impeller blades per impeller.
Preferably, axial pumping impeller means 43 comprises a downwardly pumping impeller means provided with impeller blades 42 (six blades in the illustrated embodiment) which are inclined (e.g. 30 to 45) to the vertical, such that when rotated about axis 41 impeller blades 42 impart a downward pumping action to fluid (liquid and gas bubbles).
Most preferably, the axial pumping impellers are positioned above the high shear mixing zone. Gas bubbles 53 introduced into the reactor 10 are introduced into, or below, the high shear mixing zone (e.g., below impeller means 45) and thereby dispersed radially outwardly and made smaller by such dispersing action, counteracting the natural coalescence of these gas bubbles which occurs as they rise from their point of introduction into the liquid mass.
These turbines are known in the art (see, e.g., Oldshue, supra, at pp 58-63 and pp. 178-181) and need not be more completely described herein.
While in the illustrated embodiment, a single impeller is employed in each of the high shear and downward pumping zones, it will be understood that a plurality of impellers and/or fluid injectors can be employed in either, or both, such zones. Therefore, if desired, high shear impeller means 45 can comprise 2 or more turbines.
Similarly, if desired, downward pumping impeller means 43 can comprise 2 or more turbines.
Preferably chlorine introduction means 50 is adapted to introduce chlorine gas at a point below the high shear impeller means 45 such that the chlorine introduction point, illustrated by 52 in Figure 1, is within the annulus formed by lower surface 14 of reactor 10, the outer periphery of turbine blades 45 and that distance from center axis 41 equal to one half the radius of impeller 45 (that is 1/4 of "Dtl" in Figure 1).
Preferably, the diameters of the first and second impellers 45 and 43, respectively, are substantially the (that i8 Dtl = Dt2), although this is not critical and, for example, the Dtl to Dt2 ratio can range from about 0.5:1 to 2:1, more generally from about 0.8:1 to 1.2:1). Preferably, Dtl and Dt2 are each from about 30 to 70%, more preferably from about 40 to 60%, and most preferably from about 45 to 55%, of internal diameter Dr of reactor 10.
The distance between upper and lower impellers 43 and 45 will generally comprise at least one reactor diameter, and more typically fr~m about 1 to 3 reactor diameters, for maximum benefit. Therefore, the distance sl will be generally from about Dr to 3Dr. (Figure 1 is not drawn to scale, and is for the purpose of illustrating the concepts herein.) Preferably, liquid reaction mixture 20 (having a liquid height Hr)~ comprising the initial charge of polymer and maleic anhydride, is mixed employing the plural zone turbine apparatus immersed in the liquid to provide at least 10 liquid turnovers and more preferably from about 10 to 100 liquid turnovers prior to the introduction of gaseous chlorine into the reactor. As used herein the "liquid turnover" is defined to be the number of times the total liquid reaction mixture theoretically completely circulates within the reactor 10 (given the reaction liquid volume and the pumping rate of the mixer(s)).
It has been found that the combination of high total mixing energy with plural zone mixing, wherein an upper mixing zone comprises at least one axial pumping zone, and preferably a downwardly pumping mixing zone, (employing, e.g., a pitched blade turbine or impeller turbine) and wherein the lower zone comprises a high shear zone (employing, e.g., at least one disk fixed blade turbine) enhances the percent high molecular weight polymer conversion, the polymer conversion efficiency, and the mole ratio of the monosubstituted to polysubstituted functionalized polymer at the low temperatures of operation which are employed in the process of this invention. The gas bubbles 53 introduced into the reactor 10 are introduced below high shear impeller 45 and dispersed radially outwardly and gas bubbles 53 are made smaller by such dispersing action, thereby counteracting the natural coalescence of these gas bubbles which occurs as they rise from their point of introduction into the liquid mass.
A particularly preferred mixing apparatus is one comprising the combination of disk fixed blade turbine (also known as a Rushton type impeller) and a downward pumping pitched blade or propeller impeller to provide sufficient energy dissipation to maximize mass transfer area and promote recirculation of chlorine gas bubbles.
The product mixtures prepared by the process of the present invention will preferably simultaneously possess (1) fm/fd ratios of at least about 2.5:1, more preferably at least about 3.0:1 and most preferably at least about 4:1 (e.g., from about 4:1 to 15:1 or more), and (2) an AI of at least 80 wt%, more preferably at least about 82 wt% (e.g., from about 82 to 98 wt%), and most preferably at least about 84 wt% (e.g., from about 84 to 90 wt%).
As used herein, the "fm/fd" ratio is defined to be the calculated weight ratio of the weight fraction ("fm") of polymer chains in the product mixture which are substituted by one acid functional groups (e.g. one succinic anhydride group when maleic anhydride is employed as reactant, or one propionic acid group when acrylic acid is employed as reactant) to the weight fraction ("fdH) of - 36 - 133589~

polymer C~A i nc in the product mixture which are substituted by two such acid functional groups. The fm/fd ratios can be determined from the following equation (Eq. IV):

(0-02)(y)-(F) fm/fd =
(F) - (O . 01)(y) wherein "y" is the wt.% active ingredient (i.e. "AI") in the product mixture of the polymer substituted with at least one acid functional group and "F" is the functionality of the product mixture (that is, the mole ratio of the moles of acid functional groups in the product mixture to the moles of polymer used in the reaction). The functionality "F" can be calculated from the expression (Eq. V):

(Mn) x (Sap. No.) F =
t56,100 x Zl] ~ ~Sap. No. x (Z2-2)]
wherein ~n is the number average molecular weight of the polymer used, "Sap. No. n is the saponification number of the product mixture (in units of mg.KOH/g., and deter~ined by ASTM Method D-94), ''Zl'' is 1 or 2 and is the number of carboxyl (-C(O)-) groups per molecule of monounsaturated carboxylic reactant used, and ''Z2'' is the molecular weight of the monounsaturated carboxylic reactant used.
For example, when the polymer comprises polyisobutylene (PIB) and the monounsaturated carboxylic reactant comprises maleic anhydride, the fm/fd ratio of the product mixture obtained in the formation of polyisobutylene substituted succinic anhydride (PIBSA), is determined by the expression (Eq. VI):

(0-02)(YsA)~FsA 133589S
fm/fd =
FSA-(o-Ol)(ysA) wherein ''YsA~ is the wt.% active ingredient (i.e., AI) in the product mixture of polymer substituted with succinic anhydride groups and FSA is the functionality of the product mixture (that is, the ratio of the succinic anhydride groups to the starting PIB) and is determined by the eXpression (Eq. VII):

(~n) x (Sap. No.) FSA = (112,200) - tSap. No. x (98-2)]

wherein ~n is the number average molecular weight of the PIB used in the formation of the product mixture and Sap. No. is the saponification number of the product mixture as defined above.
For purposes of simplifying the above calculations (Equations IV and V), no polymer chains having three or more such acid functional group substituents are considered to be present.
The wt.% active ingredient ("AI"), for a product mixture is calculated from the following equation (VIII):

W -Wt AI = x 100 Ws wherein Ws is the weight of the product mixture sample, and Wt is the weight of unfunctionalized polymer in the sample. The weight of unfunctionalized polymer is determined via a chromatographic technique. The unfunctionalized polymer component is separated from the functionalized polymer via column chromatography or high pressure liquid chromatography (HPLC), with a polar adsorbent such as Florisil~ Absorbent (U.S. Silica Company), alumina or silica using a non-polar hydrocarbon ` - 38 - 133589S

eluent such as hexane or cyclohexane. In the column chromatography techn;que, the unfunctionalized polymer is collected and its weight is determined. In the HPLC
~ec~nique, the weight of unfunctionalized polymer is deternined by a calibrated analytical detector, such as a refractive index detector. Care is taken to choose the sample, column size, and elution volume appropriately to achieve efficient separation. For example, use of 50 gms of Florisil~ Adsorbent, contained in a 2.5 cm x 50 cm glass column was found to be adequate to ensure separation for PIBSA product mixture sample sizes in the range of 0.1 to 5 gms using hexane as an eluent. Adequate separation is indicated by the appearance of a neat eluent fraction which succe~-c the unfunctionalized polymer containing fraction.
Infra-red spectroscopy (1700-1800 cm 1 region) can be conveniently used to monitor the eluent to assure the absence therein of carbonyl containing species upon completion of the separation which species would indicate presence of functionalized polymer.
Preferably, the process of the present invention is characterized by a long-chain hydrocarbon polymer conversion efficiency ("CEn) of at least about 75%, more preferably at least about 80% (e.g. from about 81 to 95%, and most preferably at least about 83% (e.g. from about 83 to about 90%), wherein the conversion efficiency is deternined by the equation (IX):

AI
CE =
F

wherein "F" and "AI" are as defined above in Equations V
and VIII, respectively. The process of this invention has been surprisingly found to form the desired products in high polymer conversion efficiencies, even at the low chlorination temperatures employed.

~ 39 ~ 1 33 58 9 5 The term "AI Ratio" as used herein is intended to refer to the multiplication product obtained by multiplying the AI (wt.%) for a given product mixture times the fm/fd ratio times 0.01. Therefore, the AI Ratio is a measure of the degree to which the given product mixture is concurrently characterized by a high AI and a high fm/fd ratio, which is desired in the process of the present invention. The product mixtures prepared by the process of this invention should possess an AI Ratio of at least 2.0:1 (e.g. from about 2.0:1 to 20:1 or higher), preferably at least about 2.5:1 (e.g. from about 2.5:1 to 20:1), more preferably at least about 3.5:1, and most preferably at least about 4.0:1 (e.g. from about 4.0:1 to 15:1).
The product mixtures prepàred by the process of this invention will be preferably also characterized by a content of sediment (i.e., insoluble by-product species which are suspended in the product mixture and which contribute to haze and/or color of the product mixture) of less than 0.05 vol%, preferably less than 0.03 vol%, and most preferably less than 0.01 vol% sediment, thereby greatly decreasing the equipment, manpower and environmental costs associated with the removal and disposal of the sediment from the product mixture. As used herein the volume % sediment in the product mixtures of the present invention is determined on a product mixture sample as withdrawn from the reaction zone, prior to filtration, or other sediment removal steps (while the product mixture is in a well mixed state) as follows: to 25 cc of the sample is added 75 cc heptane and the resulting mixture is placed in a graduated centrifuge tube which is then centrifuged at 1600 rpm for 20 minutes; the resulting sediment in the base of the centrifuge tube is then expressed in units of volume % sediment relative to the volume of the product mixture sample employed. Samples of ~ 40 - 1335895 the product mixture can be directly withdrawn from the reaction zone by a pipette, a liquid withdrawal conduit or other means.
The product mixtures prepared by the process of this invention will be generally characterized by a funct$onality "F" of less than about 1.25, e.g. from about 0.6 to 1.2, and more typically from about 0.7 to 1.15.
The process of this invention can also be employed to prepare low sediment product mixtures (e.g.
polyisobutenyl-substituted succinic acid or anhydride product mixtures) having a functionality "F" of greater than about 1.3, e.g., from about 1.3 to 3.0, more typically from about 1.4 to 2.0, containing decreased amounts of polymer degradation by-products.
A particularly preferred embodiment of the instant invention is, therefore, a process comprising contacting at a temperature of from about 60 to 220C, a reaction mixture comprising a polyolefin (preferably polybutene, having a number average molecular weight of at least about 1200, preferably at least about 1500, and more preferably from about 1,700 to 4,000) and maleic anhydride with chlorine gas ~preferably by continuously introducing chlorine gas into the lower portion of the reaction mixture) in an amount effective to provide from about 0.95 - 1.25 moles of chlorine per mole of maleic anhydride whereby at least about 60 mol %, preferably at least about 70 mol%, and most preferably at least about 90 mol%, of the total chlorine charged is charged at a reaction mixture temperature of not greater than about 170-C., and more preferably not greater than about 160C., while mixing the reaction mixture in the absence of an inert solvent with a plural zone mixing at a total mixing energy of at least 4 HP/1000 gal. (and more preferably at least 10 HP/1000 gal.) and for a time sufficient to provide a polymer conversion efficiency of at least 84% and to form a product mixture having an AI of at ~ - 41 - 1 3 35 8g~

least about 82 wt.% and containing less than 0.05 vol.%
sediment.
The long chain hydrocarbyl substituted mono- and dicarboxylic acid materials produced in accordance with the instant process may be used, E~ se, as additives for lubricating oils and fuels or as intermediates to provide additives such as dispersants for lubricating oils and fuels. Such dispersants, in lube oils, provide improved performance properties including enhanced diesel crankcase lubricant performance, improved deposit control, lube oil stability and enhanced resistance to oxidation.
The recovery of the product mixture containing the long chain hydrocarbyl substituted mono- or dicarboxylic acid materials produced by the process of this invention can be accomplished by means well known to those of skill in the art. Often, however, it is not nececc~ry to recover the product if, for example, it is to be used as an intermediate for the formation of other additive products.
In these instances, the reaction mixture can be further reacted with other reagents and reactants such as an alcohol, polyol, amine, polyamine, basically reacting metal compounds, etc. Usually, however, when such further reactions are carried out with the original reaction mixture, it is generally blown with an inert gas such as nitrogen to remove any (unreacted chlorine, hydrogen chloride or unreacted unsaturated mono- or dicarboxylic acid reactant) that may be present. If desired, the product mixture may be filtered to remove C~iment prior to further reactions.
Amine compounds useful as nucleophilic reactants for reaction with the hydrocarbyl substituted mono- and dicarboxylic acid materials are those containing at least two reactive amino groups, i.e., primary and secondary amino groups. They include polyalkylene polyamines of about 2 to 60, preferably 2 to 40 (e.g. 3 to 20) total carbon atoms and about 1 to 20, preferably 3 to 12, and most preferably 3 to 9 nitrogen atoms in the molecule.
These amines may be hydrocarbyl amines or may be hydroaarbyl amines including other y~OU~S~ e.g, hydroxy y-O~ alkoxy groups, amide ~ou~, nitriles, imidazoline ~L~U~ and the like. Hydroxy amines with 1 to 6 hydroxy ~ou~, preferably 1 to 3 hydroxy groups are particularly useful. Preferred amines are aliphatic saturated amines, including those of the general formulas:

R-N-(CH2)S N~(CH2)s N-R
R' R''' R' ~ t (I) wherein R, R', R'' and R''' are independently selected from the group consisting of hydrogen; Cl to C25 straight or branched chain alkyl radicals; Cl to C12 alkoxy C2 to C6 alkylene radicals; C2 to C12 hydroxy amino alkylene radicals; and Cl to C12 alkylamino C2 to C6 alkylene radicals; and wherein R"' can additionally comprise a moiety of the formula:

(CH2)s' lll II (II) I t~
R' wherein R' is as defined above, and wherein s and s' can be the same or a different number of from 2 to 6, preferably 2 to 4; and t and t' can be the same or different and are numbers of from 0 to 10, preferably 2 to 7, and most preferably about 3 to 7, with the proviso that the sum of t and t' is not greater than 15. To assure a facile reaction, it is preferred that R, R', R'', R''', s, s', t and t' be selected in a manner sufficient to provide the compounds of Formula I with typically at least one primary . _ 43 _ 1335895 or secondary amine group, preferably at least two primary or secondary amine ~ou~. This can be achieved by selecting at least one of said R, R', R" or R''' groups to be hydrogen or by letting t in Formula I be at least one when R"' is H or when the II moiety possesses a secondary amino group. The most preferred amine of the above formulas are represented by Formula I and contain at least two primary amine groups and at least one, and preferably at least three, secondary amine ~ou~.
Non-limiting examples of suitable amine compounds include: 1,2-diaminoethane; 1,3-diaminopropane;
1,4-diaminobutane; 1,6-diaminohexane; polyethylene amines such as diethylene triamine; triethylene tetramine;
tetraethylene pentamine; polypropylene amines such as 1,2-propylene diamine; di-(1,2-propylene)triamine;
di-(1,3-propylene) triamine;
N,N-dimethyl-1,3-diaminopropane; N,N-di-(2-aminoethyl) ethylene diamine; N,N-di(2-hydroxyethyl)-1,3-propylene diamine; 3-dodecyloxypropylamine; N-dodecyl-1,3-propane diamine; tris hydroxymethylaminomethane (THAM);
diisopropanol amine: diethanol amine; triethanol amine;
mono-, di-, and tri-tallow amines; amino morpholines such as N-~3-aminopropyl)morpholine; and mixtures thereof.
Other useful amine compounds include: alicyclic diamines such as 1,4-di(aminomethyl) cyclohexane, and heterocyclic nitrogen compounds such as imidazolines, and N-aminoalkyl piperazines of the general formula (III):

H-~7H-(CH2)pl \ I7 (CH2)-NH - H
- ~ CH2 CH2 - ~ P2 -nl n2 n3 wherein Pl and P2 are the same or different and are each integers of from 1 to 4, and nl, n2 and n3 are the same or different and are each integers of from 1 to 3. Non-limiting examples of such amines include 2-pentadecyl imidazoline; N-(2-aminoethyl) piperazine; etc.
Commercial mixtures of amine compounds may advantageously be used. For example, one process for preparing alkylene amines involves the reaction of an alkylene dihalide (such as ethylene dichloride or propylene dichl~ride) with ammonia, which results in a complex mixture of alkylene amines wherein pairs of nitrogens are joined by alkylene ~ou~s, forming such compounds as diethylene triamine, triethylenetetramine~ tetraethylene pentamine and isomeric piperazines. Low cost poly(ethyleneamines) compounds averaging about 5 to 7 nitrogen atoms per molecule are available commercially under trade names such as "Polyamine H", "Polyamine 400", "Dow Polyamine E-100", etc.
Useful amines also include polyoxyalkylene polyamines such as those of the formulae:

NH2 alkylenc ( O-alkylenc) ~JH2 (IV) where m has a value of about 3 to 70 and preferably 10 to 35; and R ~ alkylen ~ -alkylenc) ~JH2) n a (V) where "n" has a value of about 1 to 40 with the provision that the sum of all the n's is from about 3 to about 70 and preferably from about 6 to about 35, and R is a polyvalent saturated hydrocarbon radical of up to ten carbon atoms wherein the number of substituents on the R group is represented by the value of "a", which is a number of from 3 to 6. The alkylene groups in either formula (IV) or (V) may be straight or branched chains containing about 2 to 7, and preferably about 2 to 4 carbon atoms.

The polyoxyalkylene polyamines of formulas (IV) or (V) above, preferably polyoxyalkylene diamines and polyoxyalkylene triamines, may have average molecular weight$ ranging from about 200 to about 4000 and preferably from about 400 to about 2000. The preferred polyoxyal-kylene polyoxyalkylene polyamines include the polyoxyethylene and polyoxypropylene diamines and the polyoxypropylene triamines having average molecular weights ranging from about 200 to 2000. The polyoxyalkylene polyamines are commercially available and may be obtained, for example, from the Jefferson Chemical Company, Inc.
under the trade mark "Jeffamines D-230, D-400, D-1000, D-2000/ T-403", etc.
Additional amines useful in the present invention are described in U.S. Patent 3,4~5,441 A particularly useful class of amines are the polyamido and related amines disclosed in co-pending C~n~ n Serial No. 583,541, filed November 18, 1988, which comprise reaction products of a polyamine and an alpha, beta unsaturated compound of the formula:

D5 - C = C - C ~ Y (VI) wherein X is sulfur or oxygen, Y is -oD8, -SD8, or -ND (D ), and D5, D6, D7, D8 and D9 are the same or different and are hydrogen or substituted or unsubstituted hydrocarbyl. Any polyamine, whether aliphatic, cycloaliphatic, aromatic, heterocyclic, etc., can be employed provided it is capable of adding across the acrylic double bond and amidifying with for example the carbonyl group (-C(o~-) of the acrylate-type compound of formula VI, or with the thiocarbonyl group (-C(S)-) of the thioacrylate-type compound of formula VI.
The amine is readily reacted with the mono- or dicarboxylic acid material, e.g. alkenyl succinic anhydride, by heating an oil solution containing 5 to 95 wt. % of mono- or dicarboxylic acid material to about 100 to 200-C., preferably 125 to 175C., generally for 1 to 10, e.g. 2 to 6 hours until the desired amount of water is removed. The heating is preferably carried out to favor formation of imides or mixtures of imides and amides, rather than amides and salts. Reaction ratios of mono- or dicarboxylic acid material to equivalents of amine as well as the other nucleophilic reactants described herein can vary considerably, depending upon the reactants and type of bonds formed. Generally from 0.1 to 1.0, preferably about 0.2 to 0.6, e.g. 0.4 to 0.6, moles of mono- or dicarboxylic acid moiety content (e.g. grafted maleic anhydride content) is used, per equivalent of nucleophilic reactant, e.g.
amine. For example, about 0.5 mole of a pentamine (having two primary amino groups and S equivalents of nitrogen per molecule) is preferably used to convert into a mixture of amides and imides, the product formed by reacting one mole of olefin with sufficient maleic anhydride to add 1.0 moles of succinic anhydride groups per mole of olefin, i.e.
preferably the pentamine is used in an amount sufficient to provide about 0.4 mole (that is l.0/[O.SxS] mole) of succinic anhydride moiety per nitrogen equivalent of the amine.
Tris(hydroxymethyl) amino methane (THAM) can be reacted with the aforesaid acid material to form amides, imide$ or ester type additives as taught by U.K. 984,409, or to form oxazoline compounds and borated oxazoline compounds as described, for example, in U.S. 4,102,798;

4,116,876 and 4,113,639.
The adducts may also be esters derived from the aforesaid long chain hydrocarbon substituted mono- or dicarboxylic acid material and from hydroxy compounds such as monohydric and polyhydric alcohols or aromatic compounds such as phenols and naphthols, etc. The polyhydric ~ 47 ~ 133 S89S

alcohols are the most preferred hydroxy compounds.
Suitable polyol compounds which can be used include aliphatic polyhydric alcohols containing up to about 100 carbon atoms and about 2 to about 10 hydroxyl groups.
These alcohols can be quite diverse in structure and chemical composition, for example, they can be substituted or unsubstituted, hindered or llnhin~ered~ branched chain or straight chain, etc. as desired. Typical alcohols are alkylene glycols such as ethylene glycol, propylene glycol, trimethylene glycol, butylene glycol, and polyglycol such as diethylene glycol, triethylene glycol, tetraethylene glycol, dipropylene glycol, tripropylene glycol, dibutylene glycol, tributylene glycol, and other alkylene glycols and polyalkylene glycols in which the alkylene radical contains from two to about eight carbon atoms. Other useful polyhydric alcohols include glycerol, monomethyl ether of glycerol, pentaerythritol, dipentaerythritol, tripentaerythritol, 9,10-dihydroxystearic acid, the ethyl ester of 9,10-dihydroxystearic acid, 3-chloro-1, 2-propanediol, 1,2-butanediol, 1,4-butanediol, 2,3-hexanediol, pinacol, tetrahydroxy pentane, erythritol, arabitol, sorbitol, mannitol, 1,2-cyclohexanediol, 1,4-cyclohexanediol, 1,4-(2-hydroxyethyl)-cyclohexane, 1,4-dihydroxy-2- nitrobutane, 1,4-di-(2-hydroxyethyl)-benzene, the carbohydrates such as glucose, rhamnose, mannose, glyceraldehyde, and galactose, and the like, amino alcohols such as di-(2-hydroxyethyl) amine, tri-(3 hydroxypropyl) amine, N,N,-di-(hydroxyethyl) ethylenediamine, copolymer of allyl alcohol`and styrene, N,N-di-(2-hydroxylethyl) glycine and esters thereof with lower mono-and polyhydric aliphatic alcohols etc.
Included within the group of aliphatic alcohols are those alkane polyols which contain ether groups such as polyethylene oxide repeating units, as well as those polyhydric alcohol~ containing at least three hydroxyl yLOu~ at least one of which has been esterified with a mono-carboxylic acid having from eight to about 30 carbon atoms such as octanoic acid, oleic acid, stearic acid, linoleic acid, dodecanoic acid, or tall oil acid. Examples of such partially esterified polyhydric alcohols are the mono-oleate of sorbitol, the mono-oleate of glycerol, the mono-stearate of glycerol, the di-stearate of sorbitol, and the di-dodecanoate of erythritol.
A preferred class of ester containing adducts are those prepared from aliphatic alcohols containing up to 20 carbon atoms, and especially those containing three to 15 carbon atoms. This class of alcohols includes glycerol, erythritol, pentaerythritol, dipentaerythritol, tripentaerythritol, gluconic acid, glyceraldehyde, glucose, arabinose, 1,7-heptanediol, 2,4-heptanediol, 1,2,3-hexanetriol, 1,2,4-hexanetriol, 1,2,5-hexanetriol, 2,3,4-hexanetriol, 1,2,3-butanetriol, 1,2,4-butanetriol, quinic acid, 2,2,6,6-tetrakis(hydroxymethyl)-cyclohexanol, l,10-decanediol, digitalose, and the like. The esters prepared from aliphatic alcohols containing at least three hydroxyl groups and up to fifteen carbon atoms are particularly preferred.
An especially preferred class of polyhydric alcohols for preparing the ester adducts used as starting materials in the present invention are the polyhydric alkanols containing 3 to 15, especially 3 to 6 carbon atoms and having at least 3 hydroxyl groups. Such alcohols are exemplified in the above specifically identified alcohols and are represented by glycerol, erythritol, pentaerythritol, mannitol, sorbitol, 1,2,4-hexanetriol, and tetrahydroxy pentane and the like.
The ester adducts may be di-esters of succinic acids or acidic esters, i.e., partially esterified succinic acids: as well as partially esterified polyhydric alcohols or phenols, i.e., esters having free alcohols or phenolic hydroxyl radicals. Mixtures of the above illustrated esters likewise are contemplated within the scope of this invention.
The ester adduct may be prepared by one of several known methods as illustrated for example in U.S. Patent 3, 381,022. The ester adduct may also be borated, similar to the nitrogen containing adduct, as described herein.
Hydroxyamines which can be reacted with the aforesaid long chain hydrocarbon substituted mono- or dicarboxylic acid material to form adducts include 2-amino-2-methyl-1- propanol, p-(beta-hydroxyethyl)-aniline, 2-amino-1- propanol, 3-amino-1-propanol, 2-amino-2-methyl-1,3-propane-diol, 2-amino-2-ethyl-1,3-propanediol, N-(beta-hydroxypropyl)-N'-(beta-amino-ethyl)piperazine, tris(hydrocymethyl) amino-methane (also known as trismethylolaminomethane), 2-amino-1-butanol, ethanolamine, diethanolamine, triethanolamine, beta-(beta-hydroxy-ethoxy)-ethylamine and the like. Mixtures of these or similar amines can also be employed. The above description of nucleophilic reactants suitable for reaction with the hydrocarbyl substituted mono- or dicarboxylic acid or anhydride includes amines, alcohols, and compounds of mixed amine and hydroxy containing reactive functional groups, i.e. amino-alcohols.
Further aspects of the present invention reside in the formation of metal complexes and other post-treatment derivatives, e.g., borated derivatives, of the novel additives prepared in accordance with this invention.
Suitable metal complexes may be formed in accordance with known techniques of employing a reactive metal ion species during or after the formation of the present dispersant materials. Complex-forming metal reactants include the nitrates, thiocyanates, halides, carboxylates, phosphates, thio-phosphates, sulfates, and borates of transition metals so- I33589~

such as iron, cobalt, nickel, copper, chromium, manganese, molybdenum, tungsten, ruthenium, palladium, platinum, cadmium, lead, silver, mercury, antimony and the like.
Prior art disclosures of these complexing reactions may be found in U.S. Patents 3,306,908 and Re. 26,443.
Post-treatment compositions include those formed by reacting the novel additives of the present invention with one or more post-treating reagents, usually selected from the group consisting of boron oxide, boron oxide hydrate, boron halides, boron acids, sulfur, sulfur chlorides, phosphorous sulfides and oxides, carboxylic acid or anhydride acylating agents, epoxides and episulfides and acrylonitriles. The reaction of such post-treating agents with the novel additives of this invention is carried out using procedures known in the art. For example, boration may be accomplished in accordance with the teachings of U.S. Patent 3,254,025 by treating the additive compound of the present invention with a boron oxide, halide, ester or acid. Treatment may be carried out by adding about 1-3 wt.
% of the boron compound, preferably boric acid, and heating and stirring the reaction mixture at about 135C to 165C
for 1 to S hours followed by nitrogen stripping and filtration, if desired. Mineral oil or inert organic solvents facilitate the process.
The compositions produced in accordance with the present invention have been found to be particularly useful as fuel and lubricating oil additives.
When the compositions of this invention are used in normally liquid petroleum fuels, such as middle distillates boiling from about lS0- to 800~F. including kerosene, diesel fuels, home heating fuel oil, jet fuels, etc., a concentration of the additive in the fuel in the range of typically from 0.001 wt. % to 0.5 wt. %, preferably 0.005 wt. % to 0.2 wt. %, based on the total weight of the composition, will usually be employed. These additives can contribute fuel stability as well as dispersant activity and/or varnish control behavior to the fuel.
The compounds of this invention find their primary utility, however, in lubricating oil compositions, which employ a base oil in which the additives are dissolved or dispersed. Such base oils may be natural or synthetic.
Thus, base oils suitable for use in preparing the lubricating compositions of the present invention include those conventionally employed as crAnkcA~e lubricating oils for spark-ignited and compression-ignited internal combustion engines, such as automobile and truck engines, marine and railroad diesel engines, and the like.
Advantageous results are also achieved by employing the additives of the present invention in base oils conventionally employed in and/or adapted for use as power transmitting fluids such as automatic transmission fluids, tractor fluids, universal tractor fluids and hydraulic fluids, heavy duty hydraulic fluids, power steering fluids and the like. Gear lubricants, industrial oils, pump oils and other lubricating oil compositions can also benefit from the incorporation therein of the additives of the present invention.
Thus, the additives of the present invention may be suitably incorporated into synthetic base oils such as alkyl esters of dicarboxylic acids, polyglycols and alcohols; polyalpha-olefins, polybutenes, alkyl benzenes, organic esters of phosphoric acids, polysilicone oils, etc.
selected type of lubricating oil composition can be included as desired.
The additives of this invention are oil-soluble, dissolvable in oil with the aid of a suitable solvent, or are stably dispersible materials. Oil-soluble, dissolvable, or stably dispersible as that terminology is used herein does not nec~s~rily indicate that the ` - 52 - 133589~

materials are soluble, dissolvable, miscible, or capable of being susp~nAe~ in oil in all proportions. It does mean, however, that the additives, for instance, are soluble or stably dispersible in oil to an extent sufficient to exert their intended effect in the environment in which the oil is employed. Moreover, the additional incorporation of other additives may also permit incorporation of higher levels of a particular polymer adduct hereof, if desired.
Accordingly, while any dispersant effective amount of these additives can be incorporated into the fully formulated lubricating oil composition, it is contemplated that such effective amount be sufficient to provide said lube oil composition with an amount of the additive of typically from 0.01 to about 10, e.g., 0.1 to 6.0, and preferably from 0.25 to 3.0 wt. %, based on the weight of said composition.
The additives of the present invention can be incorporated into the lubricating oil in any convenient way. Thus, they can be added directly to the oil by dispersing, or dissolving the same in the oil at the desired level of concentration, typically with the aid of a suitable solvent such as toluene, cyclohexane, or tetrahydrofuran. Such blending can occur at room temperature or elevated.
Natural base oils include mineral lubricating oils which may vary widely as to their crude source, e.g., whether paraffinic, naphthenic, mixed, paraffinic-naphthenic, and the like; as well as to their formation, e.g., distillation range, straight run or cracked, hydrofined, solvent extracted and the like.
More specifically, the natural lubricating oil base stocks which can be used in the compositions of this invention may be straight mineral lubricating oil or distillates derived from paraffinic, naphthenic, asphaltic, or mixed base crudes, or, if desired, various blends oils ~ 53 ~ 133S89S

may be employed as well as residuals, particularly those from which asphaltic constituents have been removed. The oils may be refined by conventional methods using acid, alkali, and/or clay or other agents such as aluminum chloride, or they may be extracted oils produced, for example, by solvent extraction with solvents of the type of phenol, sulfur dioxide, furfural, dichlorodiethyl ether, nitrobenzene, crotonaldehyde, etc.
The lubricating oil base stock conveniently has a viscosity of typically about 2.5 to about 12, and preferably about 2.5 to about 9 cSt. at lOO-C.
Thus, the additives of the present invention can be employed in a lubricating oil composition which comprises lubricating oil, typically in a major amount, and the additive, typically in a minor amount, which is effective to impart enhanced dispersancy relative to the absence of the additive. Additional conventional additives selected to meet the particular requirements of a temperatures. In this form the additive per se is thus being utilized as a 100% active ingredient form which can be added to the oil or fuel formulation by the purchaser.
Alternatively, these additives may be blended with suitable oil-soluble solvent and base oil to form concentrate, which may then be blended with a lubricating oil base stock to obtain the final formulation. Concentrates will typically contain from about 2 to 80 wt. %, preferably from about 10 to 60 wt.%, and more preferably from about 5 to 40% wt.% of the additive.
The lubricating oil base stock for the additive of the present invention typically is adapted to perform selected function by the incorporation of additives therein to form lubricating oil compositions (i.e., formulations).
Representative additives typically present in such formulations include viscosity modifiers, corrosion inhibitors, oxidation inhibitors, friction modifiers, other ~icpersants, anti-foaming agents, anti-wear agents, pour point depressants, detergents, rust inhibitors and the like.
In the following experiments, all parts and percentages are on a weight basis unless otherwise indicated. Molecular weights are number average molecular weights. HPIB~ refers to polyisobutylene, and "PIBSA"
refers to product mixture containing polyisobutylene substituted with succinic anhydride groups. In the Runs that follow, the AI is determined by calculation from the weight of unfunctionalized polyisobutylene polymer which is determined in the product mixture of each Run. The Saponification Numbers (Sap. No.) are reported in units of mg KOH per g and are determined by hydrolyzing the anhydride groups in the PIBSA product mixture to the acid moiety, and reacting the resulting carboxyl groups with KOH
according to ASTM Method D-94. The F values, fm/fd ratios, AI ratios and polymer conversion efficiencies (CE) are determined as described above.

Into a non-baffled stirred tank lab reactor (equipped with a non-refluxing overhead condenser) are charged 2,800 parts of polybutene (~w/~n = 2.5) having a number average molecular weight of 2,225 and 170 parts of maleic anhydride. The resultant reaction mixture is heated to 120C. with stirring at a total mixing energy of about 14 HP/1000 gal. Thereafter, the stirring is continued and the reaction mixture is heated as follows:
heat at an even rate from 120 to 220C over 2 hours; and hold at 220C for 5 hours (for a total reaction time of 7 hours). Into the stirred reaction mixture is continuously charged 134.7 parts of chlorine at an uniform rate over a period of 6 hours, with the chlorine charge being begun when the reaction mixture temperature has reached 120C, such that about 15 mole % of the total chlorine charge is introduced at a temperature of not greater than about 170C., and about 10 mol % of the total chlorine charge is introduced at a temperature of not greater than 150-C. One hour after the chlorine charge is completed, the reaction mixture is sparged with gaseous nitrogen at 220C for 1.5 hours.

Run 2 The procedure of Run 1 is repeated except that the reaction temperature is increased from 120 to 220C over a period of 4 hours, such that about 30 mole % of the total chlorine charge is introduced at a temperature of not greater than about 170C, and about 15 mole % is introduced at 150C or below.

Run 3 The procedure of Run 1 is repeated except that the the reaction mixture is heated employing the following temperature profile: heat at an even rate from 120 to 150C
over 1 hour; hold at 150C for one-half hour; heat to 170C
over one-half hour; hold at 170C for 2 hours; heat to 220C over 3 hours; hold at 220C for 0.5 hour, for a total reaction time of 7.5 hours. Again, the chlorine charge is begun when the reaction mixture temperature reaches 120C.
1.5 hours after the chlorine charge is completed, the reaction mixture is sparged with gaseous nitrogen at 220C
for 1.5 hours. Therefore, about 70 mole % of the total chlorine charge is introduced at a temperature of not greater than about 170C, and about 25 mole % of the total chlorine charge is introduced at a temperature of not greater than about 150C.

133~89~

Run 4 The procedure of Run 3 is repeated except that the following temperature profile is used: heat at an even ratio from 120 to lSO-C over 1 hour; hold at 150C for one-half hour; heat at an even rate to 170C over one-half hour; hold at 170C for 4 hours; heat to 220C over 2 hours; hold at 220C for 2 hours, for a total reaction time of 8.5 hours. 2.5 Hours after the chlorine charge is completed, the reaction mixture is sparged with gaseous nitrogen at 220C for 1.5 hours. Therefore, 100 mole % of the total chlorine charge is introduced at a temperature of not greater than about 170C, and about 25 mole % of the total chlorine charge is introduced at a temperature of not greater than about 150C.
The data obtained in Runs 1-4 are summarized in Table I below.

TABLE I
Mole%
Run C12 Sap. A.I. ~n~. Y fd Sol~Est AI
No. < 170C No.* (Wt.%) F* Eff. ratio* (Vol. %)* Ratio*

1 15 55.5 78.2 1.15 68 1.12 0.88 0.88 2 33 52.0 75.0 1.08 69 1.27 0.68 0.95 3 70 48.5 80.0 1.01 79 2.80 0.20 2.24 4 100 49.5 80.6 1.03 78 2.59 0.28 2.09 *Reported data, for each Run, represents the average of two experiments at the indicated conditions.

The data in Table I show that as the percent of the total chlorine, introduced at 170C or below (herein termed "low temperature chlorine charge" for convenience) is increased from 15 mol% to 33 mol%, and still further to mole %, at these high total mixing conditions, an 133589~

appreciable increase in the conversion efficiency, the fm/fd ratio, and the wt.% active ingredient is observed. The decrease in the wt.% active ingredients (75.0% in Run 2 vs. 78.2% in Run 1), observed in increasing the low temperature chlorine charge to 33 mol% from 15 mol%, is surprisingly reversed as the low temperature chlorine charge is increased still further to 70-100 mol%.
Active ingredient concentrations of about 80-81% are observed in Runs 3-4.
Further, as the percent of such low temperature chlorine charge is increased from 15 to 70 mole %, the quantity of sediment by-product produced decreases. It should be noted that more maleic anhydride has reacted in Runs 1-2 than in Runs 3-4, resulting in higher Sap. Nos.
for Runs 1-2, despite the lower polyisobutylene conversion efficiencies in Runs 1-2. This indicates that the products of Runs 1-2 contain more of the polyfunctional species of the long chain hydrocarbyl substituted dicarboxylic acid material than the products of Runs 3-4. Though high maleic anhydride conversions are generally desirable, they are not critical because the volatility of maleic anhydride allows unreacted maleic anhydride to be easily removed from the reaction product mixture. On the other hand, polyisobutylene unfunctionalized (with maleic anhydride) cannot be practically separated from the reaction product mixture, and it is therefore incorporated and remains part of the final product sometimes adversely impacting its properties, e.g., viscometrics and economics. Furthermore, at equivalent Sap. Nos., the differences between the products produced by the process of Runs 1-2 and Runs 3-4 would be further magnified.

Run 5 Into a non-baffled stirred tank lab reactor equipped with a non-refluxing overhead condenser is charged - 58 - 133589~

1,000 parts of polyisobutylene having a number average molecular weight of 2,214 and 66.2 parts of maleic anhydride. The resulting reaction mixture is thoroughly mixed with a total mixing energy of about 6 HP/l,000 gallons. The reaction mixtures heated employing the following temperature profile: heat at an even rate from 120 to 220-C over 4 hours; hold at 220C for 3 hours; and nitrogen strip at 220C for 1.5 hours, for total reaction time of 8.5 hours. Into the stirred reaction mixture is continuously charged 54.5 parts of chlorine at a uniform rate over a period of six hours, with the chlorine charge being begun when the reaction mixture temperature has reached 120C, such that about 17 mole % of the total chlorine charge is introduced at a temperature of not greater than about 170-C.

Run 6 The procedure of Run 5 is repeated except that 60.7 parts of maleic anhydride and 48.1 parts of chlorine are used, and the reaction temperature profile is as follows: heat at an even rate from 120-145C over one hour; hold at 145C for one-half hour; heat at an even rate from 145C to 170C over one-half hour; hold at 170C for two hours; heat at an even rate from 170-220C over three hours; hold at 220C for one-half hour; and nitrogen strip at 220-C for 1.5 hours, for total reaction time of nine hours. Therefore, about 33 mole ~ of the total chlorine charge is introduced at a temperature of not greater than about 170C.

Run 7 The procedure of Run 5 is repeated except that the reaction temperature profile is as follows: heat at an even rate from 120 to 220C over 2 hours; hold at 220C for 5 hours; and nitrogen strip at 220C for 1.5 hours, for total ~ 59 ~ 1 3 35895 reaction time of 8.5 hours. Therefore, about 67 mole % of the total chlorine charge is introduced at a temperature of not greater than about 170-C.

Run 8 The p~oced~re of Run 5 i~ repeated except that the following temperature profile is employed: heat at an even rate from 120-145-C over one hour; hold at 145-C for one-half hour; heat at an even rate from 145-C to 170C
over one-half hour; hold at 170-C for four hours; heat at an even rate from 170-220-C over two hours; hold at 220C
for one-half hour; and nitrogen strip at 220C for 1.5 hours, for total reaction time of 10 hours. Therefore, about 100 mole % of the total chlorine charge is introduced at a temperature of not greater than about 170C.

The product mixtures of in Runs 5 - 8 are characterized and the data thereby obtained are summarized in Table II below:

TABLE II

Mole%
Run C12 Sap. A.I. ~x~. f~fd S31~Ert AI
No. < 170C No. (Wt.%) F Eff. ratio (Vol. %) Ratio 517 49.3 79.8 1.02 78 2.59 0.5 2.07 633 44.5 74.5 0.92 81 3.25 0.6 2.42 767 48 81.6 0.99 82 3.68 0.15 3.01 8100 44 81.3 0.91 89 7.28 0.12 6.00 As in Table I, the data of Table II show that as the low temperature chlorine charge is increased from 17 mol% or 33 mol% to 67 mol% or 100 mol%, at these high total mixing energy conditions, a significant increase in 13358g5 conversion efficiency, wt% active ingredient, fm/fd ratio and AI Ratio results, and a significant decrease in the sediment formed is also obtained. Again, as in Table I, a decrease in the wt% active ingredient concentration is observed (74.5% in Run 6 vs. 79.8% in Run 5) as the low temperature chlorine charge is increased from 17 to 33 mol%. Improved, high wt% active ingredient concentrations (81.3-81.6%) are obtained in Runs 7 and 8 in which the low temperature chlorine charge is 67 and 100 mol%, respectively.

Runs 9-11 Into a large baffled wall stirred tank reactor, provided with a partial reflux overhead condenser, in a series of runs is charged 18,160 parts of polyisobutylene having a number average molecular weight of 2,225 and 320 parts of maleic anhydride. The resultant reaction mixture is thoroughly mixed with a mixing energy of about 10 HP/1000 gal. employing a dual flight retreat blade stirrer, comprising an upper retreat blade impeller and a lower retreat blade impeller. The temperature of the reaction mixture is increased at an even rate over a period of 6 hours from 120C to 220C (i.e., the heat-up period) and held at 220-C for 1 hour. The reaction mixture is then nitrogen stripped for 2 hours. An additional 740 parts of maleic anhydride is charged at a uniform rate to the reaction mixture over the first 2 hours of the heat-up period. 898 parts of gaseous chlorine is continuously charged to the reaction mixture at a uniform rate during the first 5 hours of the heat-up period such that about 60 mole % of the total chlorine charged is added to the stirred reaction mixture at a temperature of not greater than about 170C.

Runs 12-13 The procedure of Run 9 is repeated in two runs except that the reactor comprises a large baffled wall stirred tank reactor, provided with a partial reflux overhead con~encer and equipped with a dual flight vertical flat blade turbine (comprising an upper vertical flat blade impeller and a lower vertical flat blade impeller), and the total mixing energy is about 11 HP/1000 gal.

Run 14 The procedure of Run 9 is repeated except that the reactor employs a dual zone stirrer (an upper pitched blade turbine and a lower disk flat blade turbine) to provide an upper axial pumping zone and a lower high shear zone at a total mixing energy of about 18 HP/1000 gals., and except that the total maleic anhydride and chlorine charges are adjusted to provide a maleic anhydride:PIB mole ratio of 1.11:1 and a C12:maleic anhydride mole ratio of 1.27:1.

Run 15 The procedure of Run 14 is repeated.

Run 16 The procedure of Run 14 is repeated except that the total mixing energy is about 15 HP/1000 gal.

The product mixtures of Runs 9 - 16 are analyzed, and the results thereby obtained are summarized in Table III below:

- 62 - 1 3~589S

TABLE III

Mole%
Run C12 Sap. A.I. Ccnv. Y fd Sel~Ert Al No. < 170C No. (Wt.%) F Eff. ratio (Vol. ~) Ratio 9 60 48.5 75.2 1.00 75 2.01 0.15 1.51 47.6 73.7 0.98 74 1.98 -- 1.46 11 60 47.7 75.6 0.98 76 2.29 -- 1.73 12 60 48.0 80.5 0.99 80 3.28 0.01 2.63 13 60 49.0 79.5 1.01 80 2.65 -- 2.11 14 80 45.5 83.3 0.94 89 6.8 0.02 5.6 47.8 83.8 0.99 85 4.5 0.02 3.8 16 80 48.7 86.7 1.01 86 5.1 0.02 4.4 As illustrated by the data in Table III for Runs 9-13, at constant low temperature chlorine charge conditions, increasing the high total mixing energy results in increased polymer conversion efficiencies, AI and fm/fd ratios, and hence in the AI Ratio factors.
Further, in comparing Runs 14-16, it can be seen that the use of dual zone high total mixing energy stirring in combination with low chlorination temperatures achieved still higher wt.% active ingredient concentrations, higher polymer conversion efficiencies, higher fm/fd ratios and higher AI Ratios, without sacrificing the low sediment levels obtained in Run 12.

Run 17 Into a baffled stirred tank pilot plant reactor vessel equipped with a partial reflux overhead condenser are charged 544 parts of polyisobutylene having a number average molecular weight of 2225 and 30 parts of maleic anhydride. The resultant reaction mixture is thoroughly ~ - 63 -mixed using a single disk flat blade turbine with a total mixing energy of about 17 HP/1000 gal. The temperature of the reaction mixture is increased at an even rate over a period of 5 hours from 120-C. to 220-C. and held at 220C.
for one hour. Then, the reaction mixture is sparged with nitrogen for 1.5 hours to remove unreacted maleic anhydride. During the 5 hours of increasing the temperature from 120C. to 220C., and the one hour soak period at 220-C., 25 parts of chlorine are continuously introduced into the stirred reaction mixture at a uniform rate in a manner such that about 40 mole % of the chlorine is added to the reaction mixture at a temperature of not greater than about 170C.

Run 18 Into the reactor vessel as used in Run 17 are charged 544 parts of polyisobutylene having a number average molecular weight of 2225 and 30 parts of maleic anhydride. The resultant reaction mixture is thoroughly mixed using a single disk flat blade turbine with a total mixing energy of about 22 HP/1000 gal. The temperature of the reaction mixture is increased at an even rate from 120 to 170C. over a period of 2 hours, held at 170C. for 2.5 hours, then increased at an even rate up to 220C. over a period of 1.5 hours, and the reaction mixture is then sparged with nitrogen for 1.5 hours. During the first five hours of this reaction sequence 25 parts of chlorine are uniformly introduced into the reaction mixture in a manner such that 90 mole % of the chlorine is added to the reaction mixture at a temperature of not greater than about 170C.
The Sap. No., AI, F, fm/fd ratio, and volume %
sediment found in Runs 17-18 are determined and the results are set forth in Table IV.

` - 64 - 1 33589S
TART~ IV

Mole%
Run HP/ C12 Sap. A.I. ~n~. y fd Solh~nt Al No. 1~ Gal. < 170-C No. (Wt.%) F Tff. ratio (Vol. %) Ratio 17 17 40 44 64.5 0.91 71 1. 43 0.06 0.92 18 22 90 42 80.0 0.86 93 11.5 0.04 9.2 The data in Table IV also indicate the effect upon the polymer conversion efficiency, fm/fd ratio, AI and, hence, the AI Ratio of concurrently increasing the low temperature chlorine charge and total mixing energy.

Run 19 Into a non-baffled stirred tank lab reactor equipped with a non-refluxing overhead condenser is charged 1,000 parts of polyisobutylene having a number average molecular weight of 2,214 (~w/~n 2.04) and 66 parts of maleic anhydride. The resultant reaction mixture is thoroughly mixed using a single vertical flat blade turbine with a total mixing energy of about 24 HP/l,000 gallons. Thereafter, the stirring is continued and the temperature of the reaction mixture is increased at an even rate over a period of 8 hours from 120- from 120C
to 220-C (i.e., the heat-up period) and is then nitrogen stripped for 1. 5 hrs. at 220C. 55 parts of gaseous chlorine is continuously charged to the reaction mixture at a uniform rate during the first 4 hours of the heat-up period such that about 100 mole % of the total chlorine charge is added to the stirred reaction mixture at a temperature of not greater than about 170C.

Run 20 The procedure of Run 19 is repeated except that 69 parts of maleic anhydride and 59.5 parts of chlorine are employed. Again, the rate of introduction of the chlorine is such that 100 mole % of the total chlorine charged is added to the stirred reaction mixture and the temperature of not greater than about 170-C.

Run 21 The procedure of Run 19 is repeated except that 72 parts maleic anhydride and 64 parts of chlorine are employed. Therefore, 100 mole ~ of the chlorine is also introduced in this reaction at temperature of not greater than about 170C.

The product mixtures of Runs 19 - 21 are characterized and are found to contain low sediment levels and high wt.% active ingredient concentrations. The data thereby obtained are summarized in Table V below:

TABLE V

Mole~
Run C12 Sap. A.I. Ox~. fm/fd SeduEnt AI
No. < 170C No. (Wt.%) F Eff. ratio (Vol. %) Ratio 19 100 49.6 84.0 1.03 82 3.43 0.03 2.88 100 53 84.4 1.10 77 2.29 0.05 1.93 21 100 55 82.9 1.14 73 1.66 0.09 1.38 Runs 22 - 24 In a series of runs, the procedure of the indicated Run is repeated to prepare the following PIBSA product mixtures (with adjusted maleic anhydride and chlorine as needed to achieve the target Sap. No.).

Table VI

Repeat HP/ Sap. ~x~. S31~Est AI
Run No. Run lK Gal. No. F Eff. (Vol.%) Ratio 223(1) 14 42 0.8689 -- 5.5 233(2) 14 48 0.9981 -- 2.5 246(3) 6 48 0.9987 0.03 4.7 (1) Repeat of procedure of Run 3, except using a maleic anhydride:PIB mole ratio of 1.10:1 and a C12:maleic anhydride mole ratio of 1.09:1.
(2) Same as (1) except using a maleic anhydride:PIB mole ratio of 1.35:1.
(3) Repeat of procedure of Run 16 using a dual zone stirrer (upper pitched blade turbine and lower disk flat blade turbine, thereby providing an upper downward-pumping zone and a lower high-shear zone) at a total mixing energy of about 6 HP/1000 gal., except that the total maleic anhydride and chlorine charges are adjusted to provide a maleic anhydride:PIB mole ratio of 1.19:1 and a C12:maleic anhydride mole ratio of 1.08:1, and the chlorine injection rate and temperature profile is such that 70 mole % of the chlorine is charged at a temperature of not greater than about 170C.

Therefore, at least 70 mol% of the total C12 charge in each of Runs 22-24 is introduced into the reaction liquid at a temperature of not greater than 170~C.

Runs 25-30: Preparation of Dispersant A series of polyisobutylene succinimide dispersants are prepared by contacting a polyethylene polyamine, having an average of 5 nitrogen atoms per molecule, with the polyisobutylene-substituted succinic anhydride product mixtures which are formed as in Runs 18 or 22 - 24 above, at the selected mol ratio of the polyethylene polyamine to the polyisobutylene-substituted succinic anhydride product.
The reactions to form the dispersants are conducted by contacting the reactants at a temperature of 150 C for 1 hour with stirring under N2, followed by sparging with N2 for 1.5 hours, and filtering. The dispersants are each then borated by reaction with boric acid over two hours at 163-C, followed by 2 hours of N2 stripping, then cooling and filtering to give the final product, to provide a boron content in the borated dispersant product mixture of about 0.2 wt% and a nitrogen content of about 0.9 wt%.
The borated dispersants thereby obtained are then formulated into a series of lOW40 lubricating oil compositions, at a constant nitrogen concentration, which oils each also contained the equivalent amounts of hydrocarbon type viscosity index improver, a zinc dialkyl dithiophosphate antiwear additive, an overbased 400 TBN
magnesium sulfonate detergent additive, and anti-friction additive, an antioxidant and an àntifoamant.
The lubricating oils thereby obtained are tested in a Caterpillar l-H2 Test, but for 120 hours rather than the full 480 hour test described in ASTM Document for Single Cylinder Engine Test for Evaluating the Performance of Crankcase Lubricants, Caterpillar l-H2 Test Method, Part 1, STP S09A. This test evalutes the ability of diesel lubricants to curtail accumulation of deposits on the piston when operating in high severity diesel engines.
The results are shown in Table VII below.

TABLE VII
Caterpillar l-H2 Test - 120 Hours lOW40 Lubricants PIBSA
From Sap. AI Yfd AI SA:
Test Run No. ~k.%) On~. Ratio Ratio PN T&F WTD
0~ No. (1) (2)Eff.(2~ (2) (2) (3) (4) (5) 18 42 80 93 11.5 9.2 0.30 3 58.6 26 18 42 80 93 11.5 9.2 0.63 18 43.5 27 22 42 77 89 7.2 5.5 0.30 17 91.7 28 22 42 77 89 7.2 5.5 0.63 20 87.9 29 23 48 80 81 3.1 2.5 0.57 42 86.4 24 48 86 87 5.5 4.7 0.57 1 16.6 tl) Saponification numbers as found for the PIBSA
product mixture used in preparation of dispersants.
(2) AI, fm/fd~ conversion efficiency and AI Ratio values as found for PIBSA product mixture charged.
(3) Ratio of equivalents of succinic anhydride groups (calculated as anhydride) charged with the polyisobutylene-substituted succinic anhydride ("PIBSA" ) to the equivalents of nitrogen atoms charged with the polyethylene polyamine in preparation of the dispersant.
(4) TGF = top groove fill (lower numbers = better results).

(5) WTD = weighted total demits (lower numbers = better results).

The above data illustrate the improved top groove fill and weighted total demerit values obtained in use of dispersant prepared from the polyisobutylene-substituted succinic anhydride product mixtures of Run 24, which is produced by the plural zone, high mixing, low temperature chlorination process of this invention, and as compared to dispersants derived from PIBSA prepared without such conditions.
The principles, preferred embodiments, and modes of operation of the present invention have been described in the foregoing specification. The invention which is intended to be protected herein, however, is not to be construed as limited to the particular forms disclosed, since these are to be regarded as illustrative rather than restrictive. Variations and changes may be made by those skilled in the art without departing from the spirit of the invention.

Claims

1. A process for preparing a product mixture containing long chain hydrocarbyl substituted mono- or dicarboxylic acid material which comprises contacting a reaction mixture with chlorine in a reaction zone provided with plural mixing zones comprising at least one high shear mixing zone and at least one axial pumping mixing zone, said reaction mixture comprising (A) polyolefin having a number average molecular weight of at least about 1,200, and (B) ethylenically unsaturated mono- or dicarboxylic acid material in an amount effective to provide at least about 0.5 mole of (B) charged per mole of (A) charged;
wherein said reaction mixture is mixed employing a total mixing energy of at least about 4 HP/1000 gal. at least during contacting of said chlorine therewith, wherein at least about 60 mole % of the total amount of chlorine employed in said process is contacted with said reaction mixture at a temperature of not greater than about 170°C., and wherein said process effects a conversion efficiency of at least about 75% at a product mixture AI of at least about 80 wt.%.

2. The process according to claim 1 wherein said ethylenically unsaturated material is selected from (i) monounsaturated C4 to C10 dicarboxylic acids wherein (a) the carboxyl groups are vicinal, and (b) at least one of said adjacent carbon atoms are part of said monounsaturation, and (ii) derivatives of (i) selected from anhydrides and C1 to C5 alcohol derived mono- or diesters of (i).

3. The process according to claim 2 wherein said ethylenically unsaturated dicarboxylic acid material is selected from maleic acid, maleic anhydride and mixtures thereof.

4. The process according to claim 1 wherein said polyolefin comprises polybutene.

5. The process according to claim 1 wherein said polyolefin has a number average molecular weight of at least about 1500.

6. The process according to claim 5 wherein said polyolefin comprises polybutene.

7. The process according to claim 5 wherein said polyolefin has a number average molecular weight of at least about 1,900.

8. The process according to claim 7 wherein said polybutene comprises polyisobutylene.

9. The process according to claim 1 wherein said reaction mixture is mixed with a total mixing energy of at least about 10 HP/1000 gal. at least during contacting of said chlorine therewith.

10. The process according to claim 9 wherein said total amount of chlorine is an amount sufficient to provide at least about 0.6 mole of chlorine per mole of (B) charged.

11. The process according to claim 10 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

12. The process according to claim 9 wherein at least about 70 mole % of said total amount of chlorine is contacted with said reaction mixture at a temperature between at least about 110°C. and not greater than about 170°C.

13. The process according to claim 9 wherein substantially all of said total amount of chlorine is contacted with said reaction mixture at a temperature between at least about 110°C., and not greater than about 170°C.

14. The process according to claim 13 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

15. The process according to claim 1 wherein at least about 70 mole % of said total amount of chlorine is contacted with said reaction mixture at a temperature not greater than about 170°C.

16. The process according to claim 15 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

17. The process according to claim 15 wherein at least about 90 mole % of said total amount of chlorine is contacted with said reaction mixture at a temperature between at least about 130°C. and not greater than about 170°C.

18. The process according to claim 17 wherein said total amount of chlorine from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

19. The process according to claim 17 wherein at least about 20 mol% of said total amount of chlorine is contacted with said reaction mixture at a temperature of not greater than about 150°C.

20. The process according to claim 19 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

21. The process according to claim 20 wherein (B) is selected from maleic anhydride, maleic acid, and mixtures thereof.

22. The process according to claim 21 wherein (A) is polybutene.

23. The process according to claim 22 wherein said polybutene has a number average molecular weight of at least about 1,500.

24. The process according to claim 23 wherein said polybutene comprises polyisobutylene having a number average molecular weight of from about 2,200 to 4,000.

25. The process according to claim 24 wherein said reaction mixture is mixed with a total mixing energy of from about 10 to 30 HP/1000 gal. at least during contacting of said chloride therewith.

26. The process according to claim 1 which further comprises thereafter elevating the temperature of the reaction mixture to from above about 170°C. to about 200°C. and contacting an amount of chlorine equal to not more than about 40 mole % of said total amount of chlorine employed in said process with said reaction mixture at said elevated temperature.

27. The process according to claim 9 which further comprises elevating the temperature of the reaction mixture to from above about 170°C. to about 200°C. and intimately contacting an amount of chlorine equal to not more than about 40 mole % of said total amount of chlorine employed in said process with said reaction mixture at said elevated temperature.

28. A process for preparing a low sediment product mixture containing long chain hydrocarbyl substituted mono- or dicarboxylic acid material which comprises contacting a reaction mixture with chlorine in a reaction zone provided with plural zone mixing comprising at least one high shear mixing zone and at least one axial pumping mixing zone, said reaction mixture comprising (A) polyolefin having a number average molecular weight of at least about 1,200, and (B) ethylenically unsaturated mono- or dicarboxylic acid material in an amount effective to provide at least about 0.5 mole of (B) charged per mole of (A) charged;
wherein said reaction mixture is mixed employing a total mixing energy of at least about 10 HP/1000 gal. at least during contacting of said chlorine therewith, wherein at least about 80 mole % of the total amount of chlorine employed in said process is contacted with said reaction mixture at a temperature of not greater than about 170°C., and wherein said process effects a polyolefin conversion efficiency of at least about 80% at a product mixture AI of at least about 80 wt.%, and wherein said product mixture contains less than about 0.05 vol.% sediment.

29. The process according to claim 28 wherein said product mixture is further characterized by a fm/fd ratio of at least about 3:1, and an AI Ratio of at least 2.5:1.

30. The process according to claim 28 wherein said ethylenically unsaturated material is selected from (i) monounsaturated C4 to C10 dicarboxylic acids wherein (a) the carboxyl groups are vicinal, and (b) at least one of said adjacent carbon atoms are part of said monounsaturation, and (ii) derivatives of (i) selected from anhydrides and C1 to C5 alcohol derived mono- or diesters of (i).

31. The process according to claim 30 wherein said ethylenically unsaturated dicarboxylic acid material is selected from maleic acid, maleic anhydride and mixtures thereof.

32. The process according to claim 28 wherein said polyolefin comprises polybutene.

33. The process according to claim 32 wherein said polybutene has a number average molecular weight of at least about 1500.

34. The process according to claim 33 wherein said polyolefin conversion is at least 84% and said AI is at least about 82 wt.%.

35. The process according to claim 33 wherein said polyolefin has a number average molecular weight of at least about 1,900.

36. The process according to claim 35 wherein said polybutene comprises polyisobutylene.

37. The process according to claim 28 wherein said reaction mixture is mixed with a total mixing energy of from about 10 to 30 HP/1000 gal. at least during contacting of said chlorine therewith.

38. The process according to claim 37 wherein said total amount of chlorine is an amount sufficient to provide at least about 0.6 mole of chlorine per mole of (B) charged.

39. The process according to claim 38 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

40. The process according to claim 37 wherein at least about 70 mole % of said total amount of chlorine is contacted with said reaction mixture at a temperature between at least about 110°C. and not greater than about 170°C.

41. The process according to claim 37 wherein substantially all of said total amount of chlorine is contacted with said reaction mixture at a temperature between at least about 110°C., and not greater than about 170°C.

42. The process according to claim 41 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

43. The process according to claim 28 wherein at least about 70 mole % of said total amount of chlorine is contacted with said reaction mixture at a temperature not greater than about 170°C.

44. The process according to claim 43 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

45. The process according to claim 43 wherein at least about 90 mole % of said total amount of chlorine is contacted with said reaction mixture at a temperature between at least about 130°C. and not greater than about 170°C.

46. The process according to claim 45 wherein said total amount of chlorine from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

47. The process according to claim 45 wherein at least about 20 mol% of said total amount of chlorine is contacted with said reaction mixture at a temperature of not greater than about 150°C.

48. The process according to claim 47 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

49. The process according to claim 48 wherein (B) is selected from maleic anhydride, maleic acid, and mixtures thereof.

50. The process according to claim 49 wherein (A) is polybutene.

51. The process according to claim 50 wherein said polybutene has a number average molecular weight of at least about 1,500.

52. The process according to claim 51 wherein said polybutene comprises polyisobutylene having a number average molecular weight of from about 2,200 to 4,000.

53. The process according to claim 52 wherein said reaction mixture is mixed with a total mixing energy of from about 10 to 30 HP/1000 gal. at least during contacting of said chloride therewith.

54. The process according to claim 28 which further comprises thereafter elevating the temperature of the reaction mixture to from above about 170°C. to about 200°C. and contacting an amount of chlorine equal to not more than about 40 mole % of said total amount of chlorine employed in said process with said reaction mixture at said elevated temperature.

55. The process according to claim 37 which further comprises elevating the temperature of the reaction mixture to from above about 170°C. to about 200°C. and intimately contacting an amount of chlorine equal to not more than about 40 mole % of said total amount of chlorine employed in said process with said reaction mixture at said elevated temperature.

56. A low sediment process for preparing a product mixture containing long chain hydrocarbyl substituted mono- or dicarboxylic acid material which comprises contacting a reaction mixture with chlorine in a reaction zone provided with plural zone mixing comprising at least one high shear mixing zone and at least one axial pumping mixing zone, said reaction mixture comprising (A) polyolefin having a number average molecular weight of at least about 1,200, and (B) ethylenically unsaturated mono- or dicarboxylic acid material in an amount effective to provide at least about 0.5 mole of (B) charged per mole of (A) charged;
wherein said reaction mixture is mixed employing a total mixing energy of at least about 4 HP/1000 gal. at least during contacting of said chlorine therewith, wherein at least about 60 mole % of the total amount of chlorine employed in said process is contacted with said reaction mixture at a temperature of not greater than about 170°C., and wherein said product mixture contains less than about 0.05 vol.% sediment.

57. The process according to claim 56 wherein said ethylenically unsaturated material is selected from (i) monounsaturated C4 to C10 dicarboxylic acids wherein (a) the carboxyl groups are vicinal, and (b) at least one of said adjacent carbon atoms are part of said monounsaturation, and (ii) derivatives of (i) selected from anhydrides and C1 to C5 alcohol derived mono- or diesters of (i).

58. The process according to claim 57 wherein said ethylenically unsaturated dicarboxylic acid material is selected from maleic acid, maleic anhydride and mixtures thereof.

59. The process according to claim 58 wherein said polyolefin comprises polybutene.

60. The process according to claim 59 wherein said polyolefin has a number average molecular weight of at least about 1500.

61. The process according to claim 59 wherein said polyolefin comprises polybutene and wherein said product mixture is chacterized by a F value of at least 1.3.

62. The process according to claim 59 wherein said polyolefin has a number average molecular weight of at least about 1,900.

63. The process according to claim 61 wherein said polybutene comprises polyisobutylene.

64. The process according to claim 63 wherein said reaction mixture is mixed with a total mixing energy of at least about 10 HP/1000 gal. at least during contacting of said chlorine therewith.

65. The process according to claim 63 wherein said total amount of chlorine is an amount sufficient to provide at least about 0.6 mole of chlorine per mole of (B) charged.

66. The process according to claim 64 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

67. The process according to claim 63 wherein at least about 70 mole % of said total amount of chlorine is contacted with said reaction mixture at a temperature between at least about 110°C. and not greater than about 170°C.

68. The process according to claim 63 wherein substantially all of said total amount of chlorine is contacted with said reaction mixture at a temperature between at least about 110°C., and not greater than about 170°C.

69. The process according to claim 67 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

70. The process according to claim 56 wherein at least about 70 mole % of said total amount of chlorine is contacted with said reaction mixture at a temperature not greater than about 170°C.

71. The process according to claim 70 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

72. The process according to claim 69 wherein at least about 90 mole % of said total amount of chlorine is contacted with said reaction mixture at a temperature between at least about 130°C. and not greater than about 170°C.

73. The process according to claim 72 wherein said total amount of chlorine from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

74. The process according to claim 71 wherein at least about 20 mol% of said total amount of chlorine is contacted with said reaction mixture at a temperature of not greater than about 150°C.

75. The process according to claim 74 wherein said total amount of chlorine is from about 0.95 to 1.25 moles of chlorine per mole of (B) charged.

76. The process according to claim 75 wherein (B) is selected from maleic anhydride, maleic acid, and mixtures thereof.

77. The process according to claim 76 wherein (A) is polybutene.

78. The process according to claim 77 wherein said polybutene has a number average molecular weight of at least about 1,500.

79. The process according to claim 78 wherein said polybutene comprises polyisobutylene having a number average molecular weight of from about 2,200 to 4,000.

80. The process according to claim 79 wherein said reaction mixture is mixed with a total mixing energy of from about 10 to 30 HP/1000 gal. at least during contacting of said chloride therewith.

81. The process according to claim 57 which further comprises thereafter elevating the temperature of the reaction mixture to from above about 170°C. to about 200°C. and contacting an amount of chlorine equal to not more than about 40 mole % of said total amount of chlorine employed in said process with said reaction mixture at said elevated temperature.

82. The process according to claim 59 which further comprises elevating the temperature of the reaction mixture to from above about 170°C. to about 200°C. and intimately contacting an amount of chlorine equal to not more than about 40 mole % of said total amount of chlorine employed in said process with said reaction mixture at said elevated temperature.