Apparatus and method for removing halogens generated during preparation of polybutene

Abstract

Disclosed are an apparatus and a method for removing halogens generated during the preparation of polybutene, which are capable of improving the utilization of polybutene and light polymers by removing halogen components contained in the polybutene and the light polymers. The method for removing halogens generated during the preparation of polybutene comprises the steps of: preparing a reaction product by supplying a catalyst and a reaction raw material to a reactor and polymerizing; removing a catalyst component from the reaction product and neutralizing; separating the reaction product into an organic compound and impurities comprising the catalyst component; heating the organic compound to distill an unreacted material; and removing a halogen component in a remaining polymerization mixture after the distillation using a halogen removing catalyst, or removing a halogen component in polybutene and light polymers obtained from the polymerization mixture using the halogen removing catalyst.

Claims

1. A method for removing halogens generated during preparation of polybutene, the method comprising: preparing a reaction product by supplying a catalyst and a reaction raw material to a reactor and polymerizing; washing a catalyst component from the reaction product and neutralizing; separating the reaction product into an organic compound and impurities comprising the catalyst component; heating the organic compound to distill an unreacted material; and removing a halogen component in a remaining polymerization mixture after the distillation using a halogen removing catalyst, or removing a halogen component in polybutene and light polymers obtained from the polymerization mixture using the halogen removing catalyst, wherein the halogen removing catalyst is iron halide selected from the group consisting of ferrous chloride (FeCl.sub.2), ferric chloride (FeCl.sub.3), ferrous fluoride (FeF.sub.2) and ferric fluoride (FeF.sub.3).

2. The method for removing halogens generated during preparation of polybutene according to claim 1, wherein a halogen content of the polymerization mixture or the light polymers after reaction with the halogen removing catalyst at 50 to 250° C. is less than 50 ppm.

3. The method for removing halogens generated during preparation of polybutene according to claim 1, wherein the form of the halogen removing catalyst is selected from the group consisting of a powder type, a spherical type, a cylindrical type and a tablet type, and the halogen removing catalyst is processed using an inorganic binder and an organic binder such that the diameter of the halogen removing catalyst is 0.1 to 100 mm.

4. The method for removing halogens generated during preparation of polybutene according to claim 1, wherein the halogen removing catalyst is obtained by dissolving iron halide in water and impregnating in aluminum oxide (Al.sub.2O.sub.3), zeolite, or clay, or by mixing the iron halide with aluminum oxide (Al.sub.2O.sub.3), zeolite, or clay.

5. The method for removing halogens generated during preparation of polybutene according to claim 1, further comprising removing halogen acid generated after removing the halogen component using a halogen acid adsorbent.

6. The method for removing halogens generated during preparation of polybutene according to claim 5, wherein the halogen acid adsorbent is 0.1 to 100 mm in the particle diameter, and the halogen acid adsorbent is selected from the group consisting of calcium hydroxide (Ca(OH).sub.2), calcium oxide (CaO), calcium carbonate (CaCO.sub.3), calcium chloride (CaCl.sub.2), potassium hydroxide (KOH), potassium carbonate (K.sub.2CO.sub.3), potassium bicarbonate (KHCO.sub.3), potassium chloride (KCl), sodium hydroxide (NaOH), sodium carbonate (Na.sub.2CO.sub.3), sodium bicarbonate (NaHCO.sub.3), solid silica, solid alumina, a strongly basic anion exchange resin and a strongly acidic cation exchange resin.

7. An apparatus for removing halogens generated during preparation of polybutene, the apparatus comprising: a reactor, into which a catalyst and a reaction raw material are supplied and polymerized to produce a reaction product; a neutralizing/washing bath for washing the catalyst from the reaction product and neutralizing the reaction product; a separating bath for separating the reaction product into an organic compound and impurities comprising the catalyst component; a C4 distillation column for distilling an unreacted material among the organic compound; and a halogen removing column for removing a halogen component in a remaining polymerization mixture after the distillation using the halogen removing catalyst, or removing a halogen component in polybutene and light polymers obtained from the polymerization mixture using the halogen removing catalyst; wherein the halogen removing catalyst is iron halide selected from the group consisting of ferrous chloride (FeCl.sub.2), ferric chloride (FeCl.sub.3), ferrous fluoride (FeF.sub.2) and ferric fluoride (FeF.sub.3).

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 is a schematic diagram illustrating an apparatus for removing halogens generated during preparation of polybutene according to an embodiment of the present invention.

DETAILED DESCRIPTION OF THE INVENTION

(2) Hereinafter, the present invention will be explained in detail referring to an attached drawing.

(3) The apparatus for removing halogens generated during preparation of polybutene according to the present invention includes, as shown in FIG. 1, (a) a reactor 10, (b) a neutralizing and washing bath 20, (c) a separating bath 30, (d) a C4 distillation column 40, and (e) a halogen removing column 42, and further includes a halogen acid adsorption column 44 and a light polymer (LP) distillation column 50.

(4) To the (a) reactor 10, a catalyst supplied from a catalyst injection line and a reaction raw material such as isobutene supplied from a raw material injection line are supplied and polymerized to produce a reaction product. The reaction product drained through the bottom of the reactor 10 is supplied to the neutralizing and washing bath 20.

(5) The catalyst is composed of a main catalyst, a cocatalyst and an auxiliary cocatalyst. The main catalyst includes a Lewis acid such as boron trifluoride, boron trichloride, aluminum trichloride and zinc chloride, the cocatalyst includes water or an alcohol compound, and the auxiliary cocatalyst includes an alkyl ether compound. The main catalyst may use a common Friedel-Craft type catalyst, without limitation, and the Lewis acid such as the boron trifluoride, the boron trichloride, the aluminum trichloride and zinc chloride may be used. However, the boron trifluoride and the aluminum trichloride, which derive terminal vinylidene well and have favorable commercial purpose are the most preferably used. The content of the boron trifluoride is 0.05 to 1 parts by weight, preferably, 0.1 to 1 parts by weight, and more preferably, 0.15 to 0.95 parts by weight on the basis of 100 parts by weight of the isobutene.

(6) The cocatalyst is essential for the reaction and functions as a proton (H.sup.+) donor for the initiation of the reaction. Water or an alcohol compound having 1 to 4 carbon atoms may be used, without limitation. The alcohol compound may include methanol, ethanol, propanol, isopropyl alcohol (isopropanol), butanol and isobutanol.

(7) In addition, the auxiliary cocatalyst is for stabilizing the protons thus generated by the cocatalyst and for controlling reactivity and includes an alkyl ether (R.sub.1—O—R.sub.2) having 2 to 10 carbon atoms, without limitation. The alkyl ether may include dimethyl ether, diethyl ether, dipropyl ether, isopropyl sec-butyl ether, sec-butyl ether, isoamyl ether, isopropyl isoamyl ether and sec-butyl isoamyl ether.

(8) Meanwhile, the injection of the catalyst is preferably an injection as a type that may easily control the quality of a product, and the main catalyst, the cocatalyst and the auxiliary catalyst may be selectively injected as a composite type of a mixture, or separately.

(9) The reaction raw material supplied via the raw material injection line and used for preparing polybutene includes 10 wt % or more, preferably 25 to 70 wt % of isobutene and may be C4 raffinate-1 remaining after the extraction of 1,3-butadiene among C4 raw materials and a butane-butene fraction (B-B fraction), which is a C4 mixture derived during separating crude oil. In the raw material, paraffin such as isobutane and normal butane, or olefin such as 1-butene, 2-butene and 30 to 50 wt % of isobutene are included. In addition, isobutene with high purity may be used after diluting using an inert organic solvent. The inert organic solvent may be isobutane, normal butane, normal pentane, isopentane and hexane, and the isobutane and the normal butane, which have similar boiling points to that of isobutene and may be easily recycled after distilling are preferably used.

(10) Referring to FIG. 1 again, in the (b) neutralizing and washing bath 20, water and a neutralizing agent injected from the transport line between the reactor 10 and the neutralizing and washing bath 20 are added to the reaction product drained from the reactor 10 to remove a catalyst component from the reaction product and neutralize. Impurities in the reaction product may be removed via washing. The reaction product from which the catalyst is removed and neutralized, is drained via the bottom of the separating bath 30. An organic compound remaining after removing the catalyst from the reaction product is drained via the top of the separation bath 30.

(11) In the (c) separating bath 30, the reaction product is separated into an organic compound and impurities including a catalyst component using a layer separation principal. The impurities including the catalyst component washed in the neutralizing and washing bath 20 is drained via the bottom of the separating bath 30, and the organic compound remaining after removing the catalyst from the reaction product is drained via the top of the separating bath 30.

(12) In the (d) C4 distillation column 40, materials such as an unreacted raw material, an inert organic solvent and a cocatalyst among the organic compounds injected from the separating bath 30 are distilled and drained via the top of the C4 distillation column 40. A remaining polymerization mixture is drained via the bottom of the C4 distillation column 40.

(13) Next, (e) the halogen removing column 42 in the apparatus for removing halogens according to the present invention is for removing the halogen component in the polymerization mixture remaining after distillation in the C4 distillation column 40, or for removing the halogen component in the polybutene and the light polymers obtained from the polymer mixture. The polymerization mixture including a halogen acid type after removing the halogen component is drained via the top of the halogen removing column 42 and is supplied to the selective apparatus of the halogen acid adsorption column 44 or the light polymer (LP) distillation column 50, which will be described subsequently.

(14) The halogen acid adsorption column 44, which may be additionally included as occasion demands, is for removing the halogen acid generated after removing the halogen component at the halogen removing column 42 using a halogen acid adsorbent filled in the halogen acid adsorption column 44. The polymer mixture from which the halogen acid is removed is supplied to a next apparatus via the top of the halogen acid adsorption column 44. In addition, the light polymer (LP) distillation column 50 is for obtaining light polymers and polybutene using the polymerization mixture from the halogen acid adsorption column 44. The light polymers are distilled and drained via the top of the light polymer (LP) distillation column 50 and transported to a light polymer (LP) storage, and the polybutene is drained to the bottom of the light polymer (LP) distillation column 50 and transported to a polybutene storage.

(15) Meanwhile, the halogen component means the chemical bond of the raw material C4 and the main catalyst such as boron trifluoride (BF.sub.3) with an organic product via a polymerization reaction, and the halogen acid is an HX type generated during removing the halogen component at the halogen removing column 42 and includes hydrogen fluoride (HF), hydrogen chloride (HCl), etc.

(16) Then, the method for removing halogens generated during preparation of polybutene according to the present invention will be explained referring to FIG. 1. FIG. 1 referred to as the following preparation method is only a method for removing halogens generated during preparation of polybutene and does not include all of the present invention.

(17) The method for removing halogens generated during preparation of polybutene according to the present invention includes a step of preparing a reaction product by supplying a catalyst and a reaction raw material to a reactor and polymerizing, a step of removing a catalyst component from the reaction product and neutralizing, a step of separating the reaction product into an organic compound and impurities including the catalyst component, a step of heating the organic compound to distill an unreacted material, and a step of removing a halogen component of the remaining polymerization mixture after the distillation using a halogen removing catalyst, or removing a halogen component of polybutene and light polymers obtained from the polymerization mixture using a halogen removing catalyst.

(18) The method for removing halogens generated during preparation of polybutene will be explained in more detail. Catalysts such as a main catalyst, a cocatalyst and an auxiliary cocatalyst, and a reaction raw material such as isobutene are supplied to the reactor 10 and polymerized to produce a reaction product. In this case, the molecular weight and the vinylidene content of a product may be determined by controlling the reaction temperature, the intensity of the catalyst, the content of isobutene after the reaction, etc. To the neutralizing and washing bath 20, water and neutralizing agent injected from the transport line between the reactor 10 and the neutralizing and washing bath 20 are added, and the catalyst component is removed from the reaction product via washing and neutralized to remove impurities in the reaction product. After that, the reaction product transported to the separating bath 30 is separated into an organic compound and impurities including a catalyst component using a layer separation principal, impurities including the catalyst component is discarded as wastewater, and the organic compound is drained and supplied to the C4 distillation column 40. In the C4 distillation column 40, the organic compound injected from the separating bath 30 is heated to distill and exhaust an unreacted raw material such as isobutene, an inert organic solvent such as isobutane and normal butane, the cocatalyst, the auxiliary cocatalyst, etc. A polymerization mixture remaining after the distillation is transported to the halogen removing column 42. Then, in the halogen removing column 42, the halogen component of the polymerization mixture remaining after the distillation in the C4 distillation column 40 may be removed using a halogen removing catalyst such as iron halide filled in the halogen removing column 42, or the halogen component of the polybutene and the light polymers obtained from the polymerization mixture may be removed using a halogen removing catalyst such as iron halide filled in the halogen removing column 42. The halogen content of the polymerization mixture or the polybutene and the light polymers after reacting with the halogen removing catalyst at a temperature of 50 to 250° C., preferably, 70 to 230° C., and more preferably, 100 to 200° C., may be less than 50 ppm, preferably, less than 30 ppm, and more preferably, less than 20 ppm. The polymerization mixture remaining after removing the halogen component is supplied to the halogen acid adsorption column 44 or the light polymer (LP) distillation column 50, which may be further included as occasion demands.

(19) Meanwhile, the halogen removing catalyst filled in the halogen removing column 42 for removing the halogen component is iron halide such as ferrous chloride (FeCl.sub.2), ferric chloride (FeCl.sub.3), ferrous fluoride (FeF.sub.2) and ferric fluoride (FeF.sub.3), and the iron halide is required to be processed into a powder type, a spherical type, a cylindrical type, a tablet type, etc. so as to be easily applied to a fixed bed reactor. The diameter is 0.1 to 100 mm, preferably, 0.5 to 97 mm, and more preferably, 1 to 95 mm. In this case, the processing may be performed using an inorganic binder of an aluminum type, a silicon type, kaolin, bentonite, etc., or an organic binder such as polyethylene glycol, polyvinyl alcohol, cellulose, wax, etc. The halogen removing catalyst may be used by a method of filling the iron halide catalyst alone in the halogen removing column 42, by dissolving the iron halide in water and impregnating in a solid acid such as aluminum oxide (Al.sub.2O.sub.3), zeolite, clay, etc., or by simply mixing the iron halide with the solid acid of the aluminum oxide, the zeolite, the clay, etc. The same effects and results may be obtained by the methods. The operating temperature of the halogen removing column 42 may be 100 to 250° C., preferably, 120 to 200° C., and more preferably, 150 to 200° C.

(20) The catalyst used for preparing polybutene includes mostly boron trifluoride and aluminum trichloride. In the case of using the two catalysts, the decrease of the halogen content (including light polymers as a by-product) in a product is limited. Accordingly, a method of removing halogens by making contact of the iron halide catalyst with polybutene and light polymers at a high temperature is essential. The method of using the iron halide is not a finite method, by which a substituted type is removed. However, the iron halide makes catalytic action, and halogens making chemical bonding to the polybutene and the light polymers may be removed as a halogen acid type. Accordingly, the life of the halogen removing catalyst may be extended. According to the iron halide compound catalyst used for removing halogens generated during preparation of polybutene, catalyst life may be extended by 10 times or more when compared to the conventional invention using only aluminum oxide, zeolite, etc.

(21) The method for removing halogens generated during preparation of polybutene will be explained. In the halogen acid adsorption column 44, which may be further included as occasion demands, halogen acids produced after removing each halogen component in the polymerization mixture, the polybutene and the light polymers in the halogen removing column 42, are removed using a halogen acid adsorbent filled in the halogen acid adsorption column 44. Halogen ion (X−), for example, fluorine ion (F−) is removed via the bonding with a metal component in the halogen acid adsorbent. In addition, in the light polymer (LP) distillation column 50, the light polymers and the polybutene may be obtained using the polymerization mixture from the halogen acid adsorption column 44. The light polymers are distilled, drained and transported to the light polymer (LP) storage, and the polybutene is also transported to a polybutene storage. The number average molecular weight (Mn) of the light polymers is from 100 to less than 300.

(22) Meanwhile, the halogen adsorbent filled in the halogen acid adsorption column 44 includes, for example, calcium hydroxide (Ca(OH).sub.2), calcium oxide (CaO), calcium carbonate (CaCO.sub.3), calcium chloride (CaCl.sub.2), potassium hydroxide (KOH), potassium carbonate (K.sub.2CO.sub.3), potassium bicarbonate (KHCO.sub.3), potassium chloride (KCl), sodium hydroxide (NaOH), sodium carbonate (Na.sub.2CO.sub.3), sodium bicarbonate (NaHCO.sub.3), solid silica, solid alumina, a strongly basic anion exchange resin, a strongly acidic cation exchange resin, etc. Among the compounds, the calcium hydroxide, the calcium oxide, the calcium carbonate, the calcium chloride, the solid silica, the solid alumina and the resins, which may form insoluble salts in water may be preferably used.

(23) The halogen acid adsorbent is required to be filled with an appropriate size so as to be easily applied to a tube shape fixed bed reactor to which a catalyst is fixed and through which a target material to be reacted is flown. The particle size (diameter) is 0.1 to 100 mm, preferably, 0.5 to 100 mm, and more preferably, 1 to 95 mm. If the halogen acid adsorbent has a diameter less than 0.1 mm and minute powder particles, the application thereof to the tube shape fixed bed reactor may be difficult, and if the diameter of the particles is greater than 100 mm, adsorption efficiency may be largely deteriorated. In addition, the particles of the adsorbent are required to be processed (molded) into a certain type, for example, spherical type, a cylinder type, a tablet type, etc. Among the types, the spherical type is the most preferable. Of course, with a continuous stirred-tank reactor (CSTR), which is a mixed flow reactor (MFR) type, all types of the catalysts may be used, however a minute powder may frequently remain in the reactor, and the CSTR is not appropriate as a reactor type.

(24) Meanwhile, polybutene is classified as highly reactive polybutene, moderately reactive polybutene and common polybutene (hereinafter, will be referred to as non-reactive polybutene). The highly reactive polybutene has the content of vinylidene at the end of a molecule of greater than 70%, preferably, 71 to 99%, more preferably, 75 to 95%, and the most preferably, 80 to 95%. The moderately reactive polybutene has the content of vinylidene at the end of a molecule of 40 to 70%, preferably, 41 to 69%, and more preferably, 45 to 65%. The non-reactive polybutene has the content of vinylidene at the end of a molecule of less than 40%, preferably, 1 to 39%, and more preferably, 5 to 35%. In addition, the reactive polybutene and the non-reactive polybutene prepared by polymerization commonly have a number average molecular weight (Mn) of 300 to 5,000.

(25) The polymerization of the highly reactive polybutene and the moderately reactive polybutene may be performed under common reaction conditions, for example, at a temperature of −40 to 20° C., and preferably, −35 to 10° C., with a pressure of 3 kg/cm.sup.2 or more, and preferably, 2.5 to 10 kg/cm.sup.2 so that reaction materials maintain a liquid state, for a retention time of 5 to 100 minutes, and preferably, 10 to 45 minutes in consideration of the costs. In addition, the conversion ratio of isobutene during polymerization of the polybutene may be 70% or more, and preferably, 80 to 95%.

(26) The polymerization of the non-reactive polybutene may be performed under common reaction conditions, for example, at a temperature of −20 to 60° C., and preferably, −10 to 50° C., with a pressure of 3 kg/cm.sup.2 or more, and preferably, 2.5 to 10 kg/cm.sup.2 so that reaction materials maintain a liquid state, for a retention time of 5 to 100 minutes, and preferably, 10 to 45 minutes in consideration of the costs. In addition, the conversion ratio of isobutene during polymerization of the polybutene may be 70% or more, and preferably, 90 to 95%.

(27) As described above, by using the apparatus and the method for removing halogens generated during preparation of polybutene according to the present invention, halogens are rarely included in the polybutene and the light polymers thus prepared. Accordingly, the polybutene may be used to form eco-friendly products, and the light polymers as a by-product may be used as a fuel additive to play the role of a friction modifier and may be applied to products with high value such as non-aromatic organic solvents or the additive of cosmetics. The effects are considerably a lot. In addition, the removal of halogens from a large amount of polymerization mixture or polybutene and light polymers may be possible due to the improvement of the mileage of the halogen removing catalyst.

MODE FOR CARRYING OUT THE INVENTION

(28) Hereinafter, the present invention will be explained in more detail referring to preferred embodiments. The following embodiments are for illustrating the present invention, and the present invention is not limited to the following embodiments.

[Preparation Example 1] Preparation of Impregnation Catalyst Filled in Halogen Removing Column

(29) To a saturated aqueous solution in which 68 g of FeCl.sub.2 was dissolved in 100 ml of water, 30 g of natural zeolite was added. After about 1 hour, the mixture thus obtained was filtered under a reduced pressure, dried under a nitrogen atmosphere at a temperature of 150° C. for 3 hours to prepare a natural zeolite catalyst impregnated with about 5% of FeCl.sub.2. Then, the catalyst was stored in a desiccator.

[Preparation Example 2] Preparation of Another Impregnation Catalyst Filled in Halogen Removing Column

(30) To a saturated aqueous solution in which 12.9 g of FeCl.sub.2 was dissolved in 100 ml of water, 30 g of natural zeolite was added to produce a mixture. Water in the mixture was distilled and removed using a rotary evaporator. The product thus obtained was dried under a nitrogen atmosphere at a temperature of 150° C. for 3 hours to prepare a natural zeolite catalyst impregnated with about 30% of FeCl.sub.2. The catalyst was stored in a desiccator.

[Example 1] Polymerization of Highly Reactive Polybutene Having Molecular Weight of 2,300 in Case of Using Halogen Removing Column Filled with FeCl2 Catalyst

(31) While maintaining the temperature of a reactor to −29° C., a composite catalyst in which the molar ratio of isopropanol (cocatalyst)/boron trifluoride (main catalyst) was 1.6 and C4-raffinate-1 which was a material having the components shown in the following Table 1 were injected to the reactor and polymerized. The pressure of the reactor was maintained to 3 kg/cm.sup.2 or more so that raw materials maintained a liquid phase, an average retention time was set to 45 minutes, and the amount of the catalyst was controlled so that the amount of the boron trifluoride was 0.27 parts by weight relative to 100 parts by weight of the isobutene. After 180 minutes, the reaction product drained from the reactor was mixed with 5 wt % of a caustic soda solution (neutralizer), and transported to a neutralizing and washing bath. The reaction was stopped and the catalyst was removed. Then, wastewater including the removed catalyst was transported to a separating bath and drained via the bottom of the separating bath. The organic compound remaining after removing the catalyst among the reaction product was drained via the top of the separating bath and injected to a C4 distillation column. The organic compound injected to the C4 distillation column was heated to 100° C., and unreacted isobutene, a cocatalyst, solvents (C4), etc. in the organic compound were distilled and removed via the top of the C4 distillation column. After that, a remaining polymerization mixture in which the amount of fluorine among the organic compound was 299 ppm passed through a halogen removing column in which 5 g of FeCl.sub.2 (halogen removing catalyst) was filled, by 40 g per hour at 200° C. to remove fluorine included in the remaining polymerization mixture. From the polymerization mixture passed through the halogen removing column, hydrogen fluoride (HF) generated at the halogen removing column was removed at the halogen acid adsorption column filled with calcium hydroxide (Ca(OH).sub.2) as a halogen acid adsorbent, and a remaining polymerization mixture was transported via the top of the halogen acid adsorption column to the light polymer (LP) distillation column. The remaining polymerization mixture supplied to the light polymer (LP) distillation column was heated under the conditions of 230° C. and 25 torr for 30 minutes, and the light polymers were distilled and drained via the top of the light polymer (LP) distillation column and transported to a light polymer (LP) storage, and the highly reactive polybutene was drained via the bottom of the light polymer (LP) distillation column and transported to a polybutene storage. The halogen removing catalyst worked for 2,420 hours, and the treatment amount of the polymer mixture (per 5 g of the halogen removing catalyst) was 96.8 kg (catalyst mileage=19,360). The molecular weight and polydispersity of the highly reactive polybutene were measured by gel permeation chromatography (GPC), vinylidene in the highly reactive polybutene was analyzed using C13-NMR, and the content of the vinylidene was 87.6%. When measuring the halogen content by an ion selective electrode (ISE) method, the fluorine content in the polybutene was 3 ppm, and the fluorine content in the light polymers was 5 ppm (Mn (number average molecular weight)=2,410, Pd (polydispersity)=1.8).

(32) TABLE-US-00001 TABLE 1 C-2- T-2- isobutene n-butane 1-butene butene butene i-butene Content 49.5 9.7 24.8 4.2 8.4 3.4 (wt %)

[Example 2] Polymerization of Highly Reactive Polybutene Having Molecular Weight of 1,000 in Case of Using Halogen Removing Column Filled with Impregnated Catalyst of Natural Zeolite with FeCl2

(33) While maintaining the temperature of a reactor to −19° C., a composite catalyst in which the molar ratio of isopropanol/boron trifluoride was 1.75 and C4-raffinate-1 which was a material having the components shown in the above Table 1 were injected to the reactor and polymerized. The pressure of the reactor was maintained to 3 kg/cm.sup.2 or more so that raw materials maintained a liquid phase, an average retention time was set to 45 minutes, and the amount of the catalyst was controlled so that the amount of the boron trifluoride was 0.33 parts by weight relative to 100 parts by weight of the isobutene. In addition, the same polymerization procedure described in Example 1 was performed except that the fluorine content in the polymerization mixture passed through the C4 distillation column was 318 ppm, and the impregnation catalyst prepared in Preparation Example 1 was used as the halogen removing catalyst of the halogen removing column to produce a product. The halogen removing catalyst worked for 300 hours, and the treatment amount of the polymer mixture was 12 kg (catalyst mileage=2,400). The vinylidene content in the highly reactive polybutene was 88.8%, the fluorine content in the polybutene was 4 ppm, and the fluorine content in the light polymers was 6 ppm (Mn=970, Pd=1.28).

[Example 3] Polymerization of Highly Reactive Polybutene Having Molecular Weight of 750 in Case of Using Halogen Removing Column Filled with Impregnated Catalyst of Natural Zeolite with FeCl2

(34) While maintaining the temperature of a reactor to −19° C., a composite catalyst in which the molar ratio of isopropanol/boron trifluoride was 1.8 and C4-raffinate-1 which was a material having the components shown in the above Table 1 were injected to the reactor and polymerized. The pressure of the reactor was maintained to 3 kg/cm.sup.2 or more so that raw materials maintained a liquid phase, an average retention time was set to 45 minutes, and the amount of the catalyst was controlled so that the amount of the boron trifluoride was 0.4 parts by weight relative to 100 parts by weight of the isobutene. In addition, the same polymerization procedure described in Example 1 was performed except that the fluorine content of the polymerization mixture passed through the C4 distillation column was 320 ppm, and the impregnation catalyst prepared in Preparation Example 2 was used as the halogen removing catalyst of the halogen removing column to produce a product. The halogen removing catalyst worked for 1,020 hours, and the treatment amount of the polymer mixture was 40.8 kg (catalyst mileage=8,160). The vinylidene content in the highly reactive polybutene was 88.2%, the fluorine content in the polybutene was 4 ppm, and the fluorine content in the light polymers was 7 ppm (Mn=770, Pd=1.23).

[Example 4] Polymerization of Highly Reactive Polybutene Having Molecular Weight of 1,000 in Case of Using Halogen Removing Column Filled with Simply Mixed Catalyst of Natural Zeolite and FeCl2

(35) While maintaining the temperature of a reactor to −19° C., a composite catalyst in which the molar ratio of isopropanol/boron trifluoride was 1.75 and C4-raffinate-1 which was a material having the components shown in the above Table 1 were injected to the reactor and polymerized. The pressure of the reactor was maintained to 3 kg/cm.sup.2 or more so that raw materials maintained a liquid phase, an average retention time was set to 45 minutes, and the amount of the catalyst was controlled so that the amount of the boron trifluoride was 0.33 parts by weight relative to 100 parts by weight of the isobutene. In addition, the same polymerization procedure described in Example 1 was performed except that the fluorine content of the polymerization mixture passed through the C4 distillation column was 302 ppm, and a mixed catalyst of 95% (4.75 g) of natural zeolite and 5% (0.25 g) of FeCl.sub.2 was used as the halogen removing catalyst of the halogen removing column to produce a product. The halogen removing catalyst worked for 310 hours, and the treatment amount of the polymer mixture was 12.4 kg (catalyst mileage=2,480). The vinylidene content in the highly reactive polybutene was 88.9%, the fluorine content in the polybutene was 3 ppm, and the fluorine content in the light polymers was 5 ppm (Mn=960, Pd=1.29).

[Example 5] Polymerization of Common Polybutene (Non-Reactive Polybutene) Having Molecular Weight of 2,400 in Case of Using Halogen Removing Column Filled with FeCl2 Catalyst

(36) While maintaining the temperature of a reactor to 0° C., a catalyst prepared as a slurry state of aluminum trichloride and non-reactive polybutene having a molecular weight of 300 and C4-raffinate-1 which was a material having the components shown in the above Table 1 were injected to the reactor and polymerized. The pressure of the reactor was maintained to 3 kg/cm.sup.2 or more so that raw materials maintained a liquid phase, an average retention time was set to 45 minutes, and the amount of the catalyst was controlled so that the amount of the aluminum trichloride was 0.014 parts by weight relative to 100 parts by weight of the isobutene. After 180 minutes, the reaction product drained from the reactor was mixed with 5 wt % of a caustic soda solution (neutralizer), and transported to a neutralizing and washing bath. The reaction was stopped and the catalyst was removed. Then, wastewater including the removed catalyst was transported to a separating bath and drained and removed via the bottom of the separating bath. The organic compound remaining after removing the catalyst among the reaction product was drained via the top of the separating bath and injected to a C4 distillation column. The organic compound injected to the C4 distillation column was heated to 100° C., and unreacted isobutene, solvents (C4), etc. in the organic compound were distilled and removed via the top of the C4 distillation column. After that, a remaining polymerization mixture in which the amount of chlorine in the organic compound was 460 ppm passed through a halogen removing column in which 5 g of FeCl.sub.2 (halogen removing catalyst) was flown, by 40 g per hour at 200° C. to remove chlorine included in the remaining polymerization mixture. From the polymerization mixture passed through the halogen removing column, hydrogen chloride (HCl) generated at the halogen removing column was removed at the halogen acid adsorption column filled with calcium hydroxide (Ca(OH).sub.2) as a halogen acid adsorbent and transported via the top of the halogen acid adsorption column to the light polymer (LP) distillation column. The remaining polymerization mixture supplied to the light polymer (LP) distillation column was heated under the conditions of at 230° C. and 25 torr for 30 minutes, and the light polymers were distilled and drained via the top of the light polymer (LP) distillation column and transported to a light polymer (LP) storage, and non-reactive polybutene was drained via the bottom of the light polymer (LP) distillation column and transported to a polybutene storage. The halogen removing catalyst worked for 1,580 hours, and the treatment amount of the polymer mixture was 63.2 kg (catalyst mileage=12,640). The chlorine content in the polybutene was 4 ppm, and the chlorine content in the light polymers was 7 ppm (Mn=2,450, Pd=1.88).

[Example 6] Polymerization of Highly Reactive Polybutene Having Molecular Weight of 1,000 in Case where Polybutene and Light Polymers Respectively Passed Through Two Halogen Removing Columns Filled with Impregnation Catalyst of Natural Zeolite with FeCl2

(37) While maintaining the temperature of a reactor to −19° C., a composite catalyst in which the molar ratio of isopropanol/boron trifluoride was 1.75 and C4-raffinate-1 which was a material having the components shown in the above Table 1 were injected to the reactor and polymerized. The pressure of the reactor was maintained to 3 kg/cm.sup.2 or more so that raw materials maintained a liquid phase, an average retention time was set to 45 minutes, and the amount of the catalyst was controlled so that the amount of the boron trifluoride was 0.33 parts by weight relative to 100 parts by weight of the isobutene. After 180 minutes, the reaction product drained from the reactor was mixed with 5 wt % of a caustic soda solution (neutralizer), and transported to a neutralizing and washing bath. The reaction was stopped and the catalyst was removed. Then, wastewater including the removed catalyst was transported to a separating bath and drained and removed via the bottom of the separating bath. The organic compound remaining after removing the catalyst among the reaction product was drained via the top of the separating bath and injected to a C4 distillation column. The organic compound injected to the C4 distillation column was heated to 100° C., and unreacted isobutene, a cocatalyst, solvents (C4), etc. in the organic compound was distilled and removed via the top of the C4 distillation column. The remaining organic compound among the organic compound, that is, the remaining polymerization mixture was transported via the bottom of the C4 distillation column to the light polymer (LP) distillation column. The remaining polymerization mixture supplied to the light polymer (LP) distillation column was heated under the conditions of 230° C. and 25 torr for 30 minutes, and the light polymers were transported to the top of the light polymer (LP) distillation column, and the highly reactive polybutene was transported to the bottom of the light polymer (LP) distillation column. The fluorine content in the transported polybutene was 25 ppm, and the fluorine content in the light polymers was 330 ppm. The polybutene and the light polymers were respectively injected to two halogen removing columns each including 5 g of the impregnation catalyst prepared in Preparation Example 1 and passed therethrough by flowing 40 g per hour at 200° C. to remove fluorine included in the remaining polybutene and the light polymers. From the polybutene and the light polymers passed through each of the halogen removing columns, hydrogen fluoride (HF) generated at the halogen removing column was removed at the halogen acid adsorption column filled with calcium hydroxide (Ca(OH).sub.2) as a halogen acid adsorbent. The halogen removing catalyst for removing the halogens of the polybutene worked for 2,860 hours, and the treatment amount of the polybutene was 114.4 kg (catalyst mileage=22,880), and the halogen removing catalyst for removing the halogens in the light polymers worked for 290 hours, and the treatment amount of the light polymers was 11.6 kg (catalyst mileage=2,320). The vinylidene content in the polybutene was 88.5%, the chlorine contents in the polybutene and the light polymers finally obtained were 3 ppm and 5 ppm, respectively (Mn=960, Pd=1.32).

[Comparative Example 1] Polymerization of Highly Reactive Polybutene Having Molecular Weight of 2,300 in Case of Using Halogen Removing Column Filled with Activated Alumina Catalyst

(38) While maintaining the temperature of a reactor to −29° C., a composite catalyst in which the molar ratio of isopropanol/boron trifluoride was 1.6 and C4-raffinate-1 which was a material having the components shown in the above Table 1 were injected to the reactor and polymerized. The pressure of the reactor was maintained to 3 kg/cm.sup.2 or more so that raw materials maintained a liquid phase, an average retention time was set to 45 minutes, and the amount of the catalyst was controlled so that the amount of the boron trifluoride was 0.27 parts by weight relative to 100 parts by weight of the isobutene. In addition, the same polymerization procedure described in Example 1 was performed except that the fluorine content of a polymerization mixture passed through the C4 distillation column was 311 ppm, the halogen removing column was filled with activated alumina (A-202HF, product of UOP Co.) as a halogen removing catalyst, and the polymerization mixture drained from the C4 distillation column was injected by 20 g per hour to the halogen removing column to produce a product. The halogen removing catalyst worked for 64 hours, and the treatment amount of the polymer mixture was 1.28 kg (catalyst mileage=256). The vinylidene content in the highly reactive polybutene was 87.4%, the fluorine content in the polybutene was 3 ppm, and the fluorine content in the light polymers was 5 ppm (Mn=2,350, Pd=1.83).

[Comparative Example 2] Polymerization of Highly Reactive Polybutene Having Molecular Weight of 1,000 in Case of Using Halogen Removing Column Filled with Zeolite Catalyst

(39) While maintaining the temperature of a reactor to −19° C., a composite catalyst in which the molar ratio of isopropanol/boron trifluoride was 1.75 and C4-raffinate-1 which was a material having the components shown in the following Table 1 were injected to the reactor and polymerized. The pressure of the reactor was maintained to 3 kg/cm.sup.2 or more so that raw materials maintained a liquid phase, an average retention time was set to 45 minutes, and the amount of the catalyst was controlled so that the amount of the boron trifluoride was 0.33 parts by weight relative to 100 parts by weight of the isobutene. In addition, the same polymerization procedure described in Example 1 was performed except that the fluorine content of a polymerization mixture passed through the C4 distillation column was 298 ppm, and the halogen removing column was filled with zeolite as a halogen removing catalyst. The halogen removing catalyst worked for 30 hours, and the treatment amount of the polymer mixture was 1.2 kg (catalyst mileage=240). The vinylidene content in the highly reactive polybutene was 88.7%, the fluorine content in the polybutene was 3 ppm, and the fluorine content in the light polymers was 5 ppm (Mn=960, Pd=1.3).

[Comparative Example 3] Polymerization of Common Polybutene (Non-Reactive Polybutene) Having Molecular Weight of 2,400 in Case of Using Halogen Removing Column Filled with Zeolite Catalyst

(40) While maintaining the temperature of a reactor to 0° C., a catalyst prepared as a slurry state of aluminum trichloride and non-reactive polybutene having a molecular weight of 300 and C4-raffinate-1 which was a material having the components shown in the above Table 1 were injected to the reactor and polymerized. The pressure of the reactor was maintained to 3 kg/cm.sup.2 or more so that raw materials maintained a liquid phase, an average retention time was set to 45 minutes, and the amount of the catalyst was controlled so that the amount of the aluminum trichloride was 0.014 parts by weight relative to 100 parts by weight of the isobutene. In addition, the same polymerization procedure described in Example 5 was performed except that the chlorine content of a polymerization mixture passed through the C4 distillation column was 440 ppm, and the halogen removing column was filled with zeolite as a halogen removing catalyst to obtain a product. The halogen removing catalyst worked for 21 hours, and the treatment amount of the polymer mixture was 0.84 kg (catalyst mileage=168). The chlorine content in the polybutene was 4 ppm, and the chlorine content in the light polymers was 7 ppm (Mn=960, Pd=1.35).

(41) In the following Table 2, polymerization mixture treatment amount, catalyst mileage and halogen content before and after removing halogens contained in the polybutene and the light polymers during the removing process of halogens according to the catalysts for removing halogens in polybutene and light polymers prepared in Examples 1 to 6 and Comparative Examples 1 to 3 are summarized.

(42) TABLE-US-00002 TABLE 2 Mixture treatment Halogen content Halogen content Halogen amount (Kg)/ before treatment after treatment removing catalyst mileage (ppm) (ppm) catalyst Polybutene LP Polybutene LP Polybutene LP Example 1 FeCl.sub.2  96.8/19,360 299 3 5 Example 2 Impregnation   12/2,400 318 4 6 catalyst (preparation example 1) Example 3 Impregnation 40.8/8,160 320 4 7 catalyst (preparation example 2) Example 4 Mixture of 12.4/2,480 302 3 5 zeolite 95% and FeCl.sub.2 5% Example 5 FeCl.sub.2  63.2/12,640 460 (Cl) 4 (Cl) 7 (Cl) Example 6 Impregnation 114.2/22,880 11.6/2,320 25 330 3 5 catalyst (preparation example 1) Comparative Activated 1.28/248   311 3 5 Example 1 alumina Comparative Zeolite 1.2/240  298 3 5 Example 2 Comparative Zeolite 0.84/168   440 (Cl) 4 (Cl) 7 (Cl) Example 3

(43) As shown in the above Table 2, it could be confirmed that the apparatus and the method for removing halogens according to the present invention had decreased halogen content and had improving effects of catalyst mileage for removing halogens as in commonly used methods (Comparative Examples 1 to 3).

(44) As described above, if dehalogenation is performed using a halogen removing column filled with a halogen removing catalyst, halogens in light polymers as a by-product may be removed as well as in polybutene generated during preparation of polybutene. The polybutene may produce an eco-friendly product due to the decrease of halogens in the polybutene. Particularly, the light polymers may produce a product with high value, unlike the light polymers without removing halogens, which should be wasted or used as a fuel oil with low price. In addition, the halogen removing catalyst used in the present invention has a merit of long life capable of being applied to a plant when compared to a conventional catalyst. Frequent replacement of a catalyst may induce difficulty in petrochemical industry and may result considerable expense, and the present invention is more meaningful.