CN112707561B - Treatment method of titanium-containing waste liquid - Google Patents
Treatment method of titanium-containing waste liquid Download PDFInfo
- Publication number
- CN112707561B CN112707561B CN201911025535.3A CN201911025535A CN112707561B CN 112707561 B CN112707561 B CN 112707561B CN 201911025535 A CN201911025535 A CN 201911025535A CN 112707561 B CN112707561 B CN 112707561B
- Authority
- CN
- China
- Prior art keywords
- titanium
- waste liquid
- distillation
- containing waste
- treating
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G23/00—Compounds of titanium
- C01G23/02—Halides of titanium
- C01G23/022—Titanium tetrachloride
- C01G23/024—Purification of tetrachloride
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The invention belongs to the field of industrial waste liquid treatment, and relates to a treatment method of titanium-containing waste liquid. The method comprises the following steps: (1) Contacting the titanium-containing waste liquid with at least one aromatic hydrocarbon to obtain a mixture; (2) Distilling the mixture in a distillation device to obtain a distillation residual liquid; (3) Mixing the distillation residual liquid with an alcohol compound for alcoholysis reaction to obtain an alcoholysis product containing hydrogen chloride; (4) Distilling the alcoholysis product to obtain an alcoholysis product with reduced chlorine content; (5) And directly carrying out solid-liquid separation on the alcoholysis product with reduced chlorine content, or carrying out neutralization reaction on the alcoholysis product with reduced chlorine content and an alkaline substance, and then carrying out solid-liquid separation to obtain organic waste liquid and solid waste residue. The method avoids scaling and blocking tendency in the distillation process of the prior method, improves the recovery rate of titanium tetrachloride, greatly reduces the generated waste water and waste residues, and has obvious environmental protection and economic benefits.
Description
Technical Field
The invention belongs to the field of industrial waste liquid treatment, and particularly relates to a treatment method of titanium-containing waste liquid.
Background
In the industrial production of polyolefin, titanium-based catalysts have been widely used because of high catalytic efficiency and low price. One common method of preparing such catalysts is to first prepare a magnesium solution, such as by reacting magnesium or a magnesium compound with a related solvent in the presence of a hydrocarbon co-agent, and then prepare a magnesium-supported catalyst by reacting the magnesium solution with a halogen-containing compound such as titanium tetrachloride, with various promoters added therebetween for modification. In the above catalyst preparation process, it is generally required to wash the obtained solid catalyst component with a hydrocarbon solvent to remove the titanium tetrachloride not carried therein, and the catalyst slurry is discharged from the reactor while producing a catalyst mother liquor containing a liquid phase material such as a hydrocarbon solvent, titanium tetrachloride and high boiling substances.
The recovery and utilization process of the polyolefin catalyst mother liquor which is industrialized at home at present is approximately as follows: the method comprises the steps of firstly, feeding a mother solution mixture containing hydrocarbon solvent, titanium tetrachloride and high-boiling substances into a mother solution rough separation tower for distillation, obtaining crude solvent from the tower top, separating titanium tetrachloride and high-boiling substances from the tower bottom through a hydrocarbon solvent rectifying tower and a titanium tetrachloride rectifying tower respectively, obtaining required hydrocarbon solvent and titanium tetrachloride products, feeding materials in the hydrocarbon solvent rectifying tower and the titanium tetrachloride rectifying tower kettle into a carbonization kettle for further distillation, dehydrating residual liquid containing titanium tetrachloride and high-boiling substances discharged from the carbonization kettle, hydrolyzing with water, neutralizing with alkali, and discharging as waste water and waste residues. Under the condition of higher recovery rate of titanium tetrachloride, the high-boiling-point substance content in the tower kettle material is higher, the material viscosity is higher when the high-boiling-point substance content is higher, the fluidity is poor, and the stay time is longer in a high-temperature state, so that the kettle wall is coked. The problems of this process are: in order to avoid stopping caused by tower blockage and kettle wall coking, the mobility of materials is ensured by reducing the recovery rate of titanium tetrachloride, so that the content of titanium tetrachloride in residual liquid discharged from the bottom of a mother liquor carbonization kettle is higher, not only is the waste of raw materials caused, but also the treatment capacity of three wastes is increased; in the hydrolysis process, a large amount of acid water containing various organic matters is generated, then neutralization treatment is carried out by alkali, and finally a large amount of waste water and waste residues are generated and need to be further treated, so that the serious environmental protection and economic pressure are faced.
There are few reports on the post-treatment of catalyst mother liquor, and the technology related to the reports comprises the adoption of a wiped film evaporator to improve the distillation efficiency, the adoption of freeze precipitation for separation and the adoption of a high-boiling point solvent to improve the recovery rate of titanium tetrachloride, but the disclosed technology has various defects in specific application. If a wiped film evaporator and a freezing precipitation method are adopted, related equipment is added on the basis of the prior art, so that the treatment cost is increased on one hand, and on the other hand, the risk of agglomeration and solidification inside the equipment exists in the deep distillation of the residue in the high-boiling residue kettle.
In addition to the above processes, there are methods currently employed to increase the recovery of titanium tetrachloride by adding a high boiling point solvent.
CN201210154391.3 discloses a method for recovering and treating a titanium-containing waste liquid, wherein the titanium-containing waste liquid is a residual liquid at the bottom of a distillation column after a titanium-containing mother liquid is treated by the distillation column, and the residual liquid contains unreacted titanium tetrachloride, alkoxy titanium and an electron donor, and the method comprises the following steps: (1) Adding a single kind of organic solvent into the titanium-containing waste liquid, and fully mixing with the titanium-containing waste liquid; the organic solvent can be well mixed with the titanium-containing waste liquid, the fluidity of the mixed liquid is good, and the organic solvent is difficult to dissolve in water; the boiling point of the organic solvent is 180-200℃: the boiling point of the organic solvent is higher than that of titanium tetrachloride and lower than that of titanium alkoxide; (2) Distilling the obtained mixed solution in a distillation device, and separating titanium tetrachloride from the top of the distillation device; the pressure of the distillation device is controlled to be normal pressure, the distillation temperature is controlled to be 137-160 ℃, and the distillation time is controlled to be 30-90 min; (3) Adding an alkali solution into the residual mixed solution in the distillation device for hydrolysis treatment, and then recovering the organic solvent.
Although the method uses a single kind of organic solvent, the boiling point of the organic solvent used is 180-200 ℃, and in particular to the examples, phenols are all used, and 8 examples are total, wherein 7 uses phenol and 1 uses o-cresol. Although this patent can greatly improve the recovery rate of titanium tetrachloride, it has the following disadvantages: firstly, the phenolic compounds are toxic substances, more importantly, the polyolefin catalyst belongs to harmful substances and is catalyst poison, and the introduction of the phenolic substances into a recovery distillation system has a potential significant risk for the preparation of the relevant catalyst. Therefore, although the method solves the local problem to a certain extent, the method has no practical application value from the aspect of the whole process.
CN201210153649.8 discloses a method for recovering refined titanium tetrachloride from titanium-containing waste liquid, which comprises the following steps: adding white oil into the titanium-containing waste liquid, and uniformly mixing; (2) Distilling the mixture in a distillation device, and separating a mixture of titanium tetrachloride and white oil from the top of the tower; (3) Rectifying the mixture of titanium tetrachloride and white oil in a rectifying device to obtain titanium tetrachloride; wherein the boiling range of the white oil is between 150 ℃ and 180 ℃): the rectification temperature is controlled to be 137-150 ℃.
Although the above process is a significant improvement over the phenolic compounds of CN201210154391.3 and the white oil used is not a poison for polyolefin catalysts, the white oil still presents a relevant potential risk for the current mainstream toluene-assisted dissolution of titanium magnesium catalyst systems (e.g. CN 200510117428.5) for those skilled in the art of actually preparing polyolefin catalysts, since if white oil is mixed into the catalyst preparation feed system the dissolution effect of magnesium compounds will be severely affected and in the dissolution of titanium magnesium catalyst preparation is an important step, so the process also has significant application limitations for the relevant catalyst preparation.
CN201110303198.7 discloses a polyolefin catalystThe treatment method of the production titanium-containing waste liquid comprises the following process steps: (1) Mixing the titanium-containing waste liquid with water according to the weight ratio of 1:0.5-1:3wt%, and performing hydrolysis treatment to obtain a hydrolysate: lime powder (Ca (OH) 2 ) Adding into a reactor, (2) transferring the hydrolysate in the step (1) into the reactor and lime (Ca (OH) 2 ) The powder is subjected to neutralization reaction, ca (OH) is controlled 2 Ratio of powder to original titanium-containing waste liquid, ca (OH) 2 The powder reacts with the hydrolysate to form solid slag. The invention adopts solid lime Ca (OH) 2 The powder is used as an alkali neutralizer, and the final treatment product is solid waste residue.
CN201110303200.0 discloses a method for recovering and treating titanium-containing waste liquid, which comprises the following steps: slaked lime (Ca (OH) 2 ) The lime milk is prepared from lime milk and water in a certain proportion in a lime milk storage tank: placing the prepared lime cream with a certain amount into a reactor: adding a certain amount of titanium-containing waste liquid into the reactor directly, controlling the adding speed of the titanium-containing waste liquid, so that the reaction temperature is not more than 90 ℃, and finally reacting to form solid waste TiO 2 /CaCl 2 ·nH 2 O。
Although the method reduces the generation of acid water to a certain extent, the obtained solid waste residue still contains a small amount of water and a large amount of organic matters, and the solid waste residue still needs to be further treated by adopting the current general method, so that the treatment process is complex.
Disclosure of Invention
Aiming at the prior art, the inventor breaks through the thought limitation of the prior art, provides a simpler, more convenient and practical method based on a brand new thought, avoids scaling and blocking tendency in the distillation process of the prior method, improves the recovery rate of titanium tetrachloride in the titanium-containing waste liquid, and uses a high-boiling point solvent which does not have adverse effect on the preparation of the catalyst, so that the integral distillation operation is easier to implement, and the related running cost is reduced; greatly reduces the waste water and waste residue generated in the treatment process, greatly reduces the chlorine content in the waste liquid, can be directly burnt, and has obvious environmental protection and economic benefits.
In order to achieve the above object, the present invention provides a method for treating a titanium-containing waste liquid, which is a titanium tetrachloride-containing waste liquid produced in a process for producing a titanium-based polyolefin catalyst, comprising the steps of:
(1) Contacting the titanium-containing waste liquid with at least one aromatic hydrocarbon to obtain a mixture, wherein the aromatic hydrocarbon has a general formula of C n H 2n-6 N is more than or equal to 20 and more than or equal to 7; preferably, 12.gtoreq.n.gtoreq.8;
(2) Distilling the mixture obtained in the step (1) in a distillation device, wherein the top of the distillation device is separated to obtain a titanium tetrachloride-containing material, and the bottom of the distillation device is obtained to obtain distillation raffinate;
(3) Mixing the distillation residual liquid obtained in the step (2) with an alcohol compound for alcoholysis reaction to obtain an alcoholysis product containing hydrogen chloride;
(4) Distilling the alcoholysis product obtained in the step (3) to remove hydrogen chloride in the alcoholysis product and obtain an alcoholysis product with reduced chlorine content;
(5) And (3) directly carrying out solid-liquid separation on the alcoholysis product with reduced chlorine content obtained in the step (4), or carrying out neutralization reaction on the alcoholysis product with reduced chlorine content and an alkaline substance, and then carrying out solid-liquid separation to obtain organic waste liquid and solid waste residue.
Compared with the prior art, the method improves the recovery rate of the titanium tetrachloride in the titanium-containing waste liquid while avoiding scaling and blocking tendency in the distillation process of the prior method, and the used high-boiling point solvent does not have adverse effect on the preparation of the catalyst, so that the integral distillation operation is easier to implement, and the related running cost is reduced; in addition, the invention adopts alcohol compounds to treat the titanium-containing waste liquid, the reaction product is a mixture of inflammable alkoxy titanium and other organic matters, after solid-liquid separation, the chlorine content of the organic waste liquid is reduced, and the waste liquid can be directly burnt, thereby really solving the dilemma that the acid-containing waste water generated in the prior art method is difficult to treat; preferably, the method further combines with alkaline substances to perform neutralization reaction, and removes hydrogen chloride contained in alcoholysis substances to further reduce chlorine content in waste liquid, so that corrosion to treatment equipment and secondary pollution such as dioxin possibly generated in the incineration process can be greatly reduced, and the method has more obvious environmental protection and economic benefits.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Detailed Description
The following describes specific embodiments of the present invention in detail. It should be understood that the detailed description and specific examples, while indicating and illustrating the invention, are not intended to limit the invention.
The invention provides a method for treating titanium-containing waste liquid, which is titanium tetrachloride-containing waste liquid generated in the preparation process of a titanium-series polyolefin catalyst, and comprises the following steps:
(1) Contacting the titanium-containing waste liquid with at least one aromatic hydrocarbon to obtain a mixture, wherein the aromatic hydrocarbon has a general formula of C n H 2n-6 N is more than or equal to 20 and more than or equal to 7; preferably, 12.gtoreq.n.gtoreq.8;
(2) Distilling the mixture obtained in the step (1) in a distillation device, wherein the top of the distillation device is separated to obtain a titanium tetrachloride-containing material, and the bottom of the distillation device is obtained to obtain distillation raffinate;
(3) Mixing the distillation residual liquid obtained in the step (2) with an alcohol compound for alcoholysis reaction to obtain an alcoholysis product containing hydrogen chloride;
(4) Distilling the alcoholysis product obtained in the step (3) to remove hydrogen chloride in the alcoholysis product and obtain an alcoholysis product with reduced chlorine content;
(5) And (3) directly carrying out solid-liquid separation on the alcoholysis product with reduced chlorine content obtained in the step (4), or carrying out neutralization reaction on the alcoholysis product with reduced chlorine content and an alkaline substance, and then carrying out solid-liquid separation to obtain organic waste liquid and solid waste residue.
The treatment object of the invention, namely titanium tetrachloride-containing waste liquid generated in the preparation process of the titanium-series polyolefin catalyst, comprises catalyst mother liquor generated in the preparation process of the titanium-series polyolefin catalyst and residual liquid containing titanium tetrachloride and high-boiling substances, which is obtained by distilling and removing part of titanium tetrachloride from the catalyst mother liquor generated in the preparation process of the titanium-series polyolefin catalyst.
According to the present invention, the aromatic hydrocarbon is preferably at least one selected from the group consisting of o-xylene, m-xylene, p-xylene, o-diethylbenzene, m-diethylbenzene, p-diethylbenzene, propylbenzene, isopropylbenzene, 1,2, 4-trimethylbenzene, 1,2, 3-trimethylbenzene, 1,3, 5-trimethylbenzene, p-methylisopropylbenzene, 1,2,3, 5-tetramethylbenzene, butylbenzene, sec-butylbenzene, tert-butylbenzene, isobutylbenzene, methylisobutylbenzene, pentylbenzene, and tert-pentylbenzene; further preferably, the aromatic hydrocarbon is at least one selected from the group consisting of propylbenzene, isopropylbenzene, 1,2, 4-trimethylbenzene, 1,2, 3-trimethylbenzene, 1,3, 5-trimethylbenzene, p-methylisopropylbenzene, sec-butylbenzene, tert-butylbenzene, isobutylbenzene and methylisobutylketone.
In order to facilitate separation from titanium tetrachloride, the aromatic hydrocarbon preferably has a boiling point of 150 to 210℃and more preferably 150 to 179 ℃.
According to the method of the present invention, the specific addition amount of the aromatic hydrocarbon varies depending on the consistency of the titanium-containing waste liquid, and preferably, the volume ratio of the aromatic hydrocarbon to the titanium-containing waste liquid is 0.05 to 5.0:1, further preferably, the volume ratio of the aromatic hydrocarbon to the titanium-containing waste liquid is 0.1 to 2.0:1.
in the step (2) of the present invention, the distillation process may be carried out by a conventional distillation method, either atmospheric distillation or vacuum distillation, preferably vacuum distillation. The present invention is not particularly limited to specific distillation conditions, and it is preferable to distill titanium tetrachloride or the corresponding aromatic hydrocarbon. Generally, the temperature of atmospheric distillation is 110 to 185 ℃, the temperature of reduced pressure distillation is 80 to 125 ℃, and the pressure is 40 to 10kPa.
The titanium tetrachloride-containing material separated from the top of the distillation device can be titanium tetrachloride or a mixture of titanium tetrachloride and aromatic hydrocarbon, and the titanium tetrachloride-containing material can further enter a rectifying tower for rectifying and recovering titanium tetrachloride, and the obtained aromatic hydrocarbon can be recycled.
In the present invention, the alcohol compound may be at least one of monohydric alcohol, dihydric alcohol and polyhydric alcohol.
Specifically, the monohydric alcohol is preferably at least one alcohol compound represented by the general formula ROH, wherein R is C 1 -C 12 Straight-chain or branched alkyl, C 3 -C 12 Cycloalkyl or C of (C) 7 -C 12 Aralkyl of (a); the monohydric alcohol is further preferably at least one of methanol, ethanol, n-propanol, isopropanol, n-butanol, isobutanol, sec-butanol, tert-butanol, n-pentanol, n-hexanol, n-heptanol, n-octanol, n-nonanol, n-decanol, cyclopentanol, benzyl alcohol, and phenethyl alcohol.
In particular, the dihydric alcohol is preferably C 2 -C 12 Is a diol of (2); further preferred are ethylene glycol and/or propylene glycol.
In particular, the polyol is preferably C 2 -C 12 Is a triol of (2); glycerol is further preferred.
In the invention, the addition amount of the alcohol compound is determined according to the volume of the distillation residual liquid to be treated, and the use amount of the alcohol compound is reduced as much as possible on the premise of meeting the requirement of alcoholysis reaction. Preferably, the volume ratio of the alcohol compound to the distillation raffinate is 0.05-15: 1, preferably 0.1 to 10:1, more preferably 0.2 to 5:1.
according to a specific treatment method of the invention: firstly, according to the actual capacity of a reaction kettle, the total volume of the materials which can be treated is obtained, and then according to the volume conversion, the corresponding addition amount of the alcohol compounds and the distillation residual liquid is obtained.
According to the present invention, in order to achieve an effect of alcoholysis better, it is preferable that in the step (1), the alcoholysis reaction is performed under stirring, and the temperature of the alcoholysis reaction is not higher than the boiling point of the alcohol compound.
Similarly to the hydrolysis process of the prior art, HCl gas is also generated during the alcoholysis process, preferably step (1) further comprises: and absorbing HCl gas generated in the alcoholysis reaction process. The HCl gas produced during the alcoholysis reaction can be neutralized and absorbed using conventional methods, for example, using water or an alkaline substance. The alkaline substance may be a common alkaline substance for neutralization, such as sodium hydroxide.
In the specific alcoholysis reaction, the distillation raffinate is added into a kettle first, and then the alcohol compound is added (namely, the alcohol compound is added into the titanium-containing distillation raffinate); or adding alcohol compound first and then adding distillation raffinate (namely adding titanium-containing distillation raffinate into the alcohol compound); preferably, the alcohol compound is added to the distillation raffinate.
According to the method of the present invention, in the step (4), the distillation treatment may be an atmospheric distillation treatment or a vacuum distillation treatment, and the number of times of distillation may be one or more times. The purpose of the distillation treatment used in the present invention is to remove hydrogen chloride therefrom, and for this purpose, one skilled in the art can select appropriate distillation treatment conditions, including: the temperature of the distillation treatment is not lower than the initial boiling point of the alcoholysis product, and the time of the distillation treatment is that the distillation is carried out until part or all of alcohol compounds in the alcoholysis product are distilled off.
According to the present invention, preferably, in the specific distillation process, step (4) further comprises: after the distillation treatment, the alcohol compound or the distillation fraction is added to the distillation product to obtain an alcoholysis product with reduced chlorine content. The distillation fraction can be recycled.
According to the present invention, the distillation treatment is preferably carried out until substantially all of the alcohol compound in the alcoholysis product is distilled off, and then the alcohol compound and/or the distillation fraction are added to the distillation product, and the above steps are repeated several times to reduce the chlorine content in the alcoholysis product. After the last distillation treatment, the alcohol compound and/or the distillation fraction is preferably still added, so as to enhance the fluidity of the alcoholysis product and facilitate the subsequent solid-liquid separation. The volume of the alcohol compound and/or the distillation fraction to be added each time is preferably such that the total volume of the system after the addition is equivalent to the total volume of the system after the first addition of the alcohol compound. Thus, in each case substantially all of the alcohol compound is distilled off, the volume of the newly added alcohol compound and/or distilled fraction is the same as the volume of the first added alcohol compound.
According to the method of the present invention, the alkaline substance is added in the step (5) for neutralizing hydrogen chloride in the alcoholysis liquid, and thus, various neutralizing bases such as hydroxides and/or oxides of alkali metals and/or alkaline earth metals, which are conventional in the art, may be selected; specifically, at least one of sodium hydroxide, potassium hydroxide, calcium hydroxide and calcium oxide may be preferable. The purpose of the neutralization is to reduce corrosion of the subsequent treatment equipment by the chloride, and therefore, the alkaline substance is preferably added in an amount to neutralize the alcoholysis liquid to neutral or weakly alkaline.
The conditions for the neutralization are not particularly limited in the present invention, and the temperature may be selected from the range of normal temperature to the boiling point of the solvent, and the addition form of the alkaline substance is preferably solid, and therefore, in order to accelerate the dissolution thereof, the neutralization reaction is preferably carried out at a relatively high temperature within a selectable range.
The method of solid-liquid separation in the present invention is not particularly limited, and may be at least one selected from the group consisting of sedimentation separation, filtration separation, press filtration separation, vacuum separation, centrifugal separation and spray-drying separation.
According to the method, the organic waste liquid with the reduced chlorine content can be directly subjected to incineration treatment, and the incineration treatment is carried out by adopting a conventional treatment mode conforming to environmental regulations. The solid waste residue can be treated in a manner conventional in the art. Such as incineration, landfill, etc.
The present invention will be further described with reference to examples, but the scope of the present invention is not limited to these examples.
Examples 1 to 8 and comparative example 1 the titanium-containing waste liquid used was a waste liquid produced in the process of preparing a polyolefin catalyst according to the following steps: in a reactor fully replaced by high-purity nitrogen, 4.03g of magnesium dichloride, 50mL of toluene, 4.0mL of epichlorohydrin, 4mL of tributyl phosphate and 6.4mL of ethanol are sequentially added, the temperature is raised to 70 ℃ under stirring, and after the solid is completely dissolved to form a uniform solution, the reaction is carried out for 1 hour at 70 ℃. The system was cooled to-5℃and 40mL of titanium tetrachloride was slowly added dropwise, followed by 3mL of tetraethoxysilane and reacted for 1 hour. Slowly heating to 80 ℃, and reacting for 2 hours. Stopping stirring, standing, quickly layering the suspension, pumping out supernatant, washing with toluene for two times and hexane for four times, and drying with high-purity nitrogen to obtain the solid catalyst with good fluidity and narrow particle size distribution. In the preparation process of the catalyst, the catalyst mother liquor of the liquid phase materials such as hydrocarbon-containing solvent, titanium tetrachloride and high-boiling substances is distilled to remove part of titanium tetrachloride, thus obtaining the titanium-containing waste liquid.
Examples 9-16 used titanium-containing waste solutions were waste solutions produced during the preparation of polyolefin catalysts according to the following procedures: in a reactor fully replaced by high-purity nitrogen, 4.03g of magnesium dichloride, 50mL of toluene, 4.0mL of epichlorohydrin, 4mL of tributyl phosphate and 6.4mL of ethanol are sequentially added, the temperature is raised to 70 ℃ under stirring, and after the solid is completely dissolved to form a uniform solution, the reaction is carried out for 1 hour at 70 ℃. The system was cooled to-5 ℃, 40mL of titanium tetrachloride was slowly added dropwise, then 3mL of silicon tetrachloride was added and reacted for 1 hour. Slowly heating to 80 ℃, and reacting for 2 hours. Stopping stirring, standing, quickly layering the suspension, pumping out supernatant, washing with toluene for two times and hexane for four times, and drying with high-purity nitrogen to obtain the solid catalyst with good fluidity and narrow particle size distribution. In the preparation process of the catalyst, the produced catalyst mother liquor of liquid-phase materials such as hydrocarbon-containing solvent, titanium tetrachloride and high-boiling substances is the titanium-containing waste liquid.
The method for testing the chlorine content in the sample is X-ray fluorescence spectrometry.
Example 1
500mL of titanium-containing waste liquid and 500mL of propylbenzene are uniformly mixed in a container, and atmospheric distillation is carried out at 110-185 ℃. When the system distillation raffinate is less than 500mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 83.6%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 100mL of methanol is gradually added under the stirring condition for reaction for 2h at 64 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with the chlorine content of 16.8wt% is obtained after the reaction is finished. And (3) carrying out normal pressure distillation on the alcoholysis product for 1 time, wherein the distillation temperature is 64 ℃, distilling until the methanol is basically completely distilled, redissolving the alcoholysis product with 100mL of methanol after the distillation is finished, and then filtering and separating to obtain an organic waste liquid with the chlorine content of 9.4wt% and a small amount of solid waste residues. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 2
Mixing 500mL of titaniferous waste liquid and 1000mL of 1,2, 4-trimethylbenzene uniformly in a container, and carrying out reduced pressure distillation at 80-125 ℃ and 40-10 kPa. When the system distillation raffinate is less than 1000mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.5%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of methanol is gradually added under the stirring condition to react for 2h at 64 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with the chlorine content of 15.9wt% is obtained after the reaction is finished. The alcoholysis product was subjected to repeated 2 times of atmospheric distillation at a distillation temperature of 64℃until substantially all of the methanol was distilled off, and after completion of each distillation, 120mL of methanol was redissolved. Then filtering and separating to obtain the organic waste liquid with the chlorine content of 7.2wt% and a small amount of solid waste. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 3
500mL of the titanium-containing waste liquid and 500mL of 1,2, 3-trimethylbenzene are uniformly mixed in a container, and atmospheric distillation is carried out at 110-185 ℃. When the system distillation raffinate is less than 500mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.8%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 100mL of methanol is gradually added under the stirring condition for reaction for 2h at 64 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with the chlorine content of 16.8wt% is obtained after the reaction is finished. The above alcoholysis product was distilled under normal pressure at a temperature of 64℃until substantially all of the methanol was distilled off, and after completion of the distillation, it was redissolved with 100mL of methanol to obtain a liquid mixture having a chlorine content of 9.4 wt%. And (3) carrying out neutralization reaction on the liquid mixture and a proper amount of sodium hydroxide solid, reacting at 64 ℃ until the solution is neutral, and then carrying out filter pressing separation to obtain the organic waste liquid and white solid waste residue with the chlorine content of 0.3 wt%. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 4
Mixing 500mL of titaniferous waste liquid and 1000mL of 1,3, 5-trimethylbenzene uniformly in a container, and carrying out reduced pressure distillation at 80-125 ℃ and 40-10 kPa. When the system distillation raffinate is less than 1000mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.2%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of methanol is gradually added under the stirring condition to react for 2h at 64 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with the chlorine content of 15.9wt% is obtained after the reaction is finished. The above alcoholysis product was subjected to repeated 2 times of atmospheric distillation at a distillation temperature of 64℃until substantially all of the methanol was distilled off, and after the completion of each distillation, 120mL of methanol was redissolved to obtain a liquid mixture having a chlorine content of 7.2% by weight. And (3) carrying out neutralization reaction on the liquid mixture and a proper amount of sodium hydroxide solid, reacting at 64 ℃ until the solution is neutral, and then carrying out filter pressing separation to obtain the organic waste liquid and white solid waste residue with the chlorine content of 0.3 wt%. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 5
500mL of titanium-containing waste liquid and 500mL of propylbenzene are uniformly mixed in a container, and atmospheric distillation is carried out at 110-185 ℃. When the system distillation raffinate is less than 500mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 83.6%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of ethanol is gradually added under the stirring condition, the reaction is carried out for 2 hours at 78 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with 13.8 weight percent of chlorine is obtained after the reaction is finished. And (3) carrying out normal pressure distillation on the alcoholysis product for 1 time, wherein the distillation temperature is 78 ℃, distilling until the ethanol is basically completely distilled, redissolving the alcoholysis product with 120mL of ethanol after the distillation is finished, and then filtering and separating to obtain an organic waste liquid with the chlorine content of 7.1wt% and a small amount of solid waste residues. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 6
Mixing 500mL of titaniferous waste liquid and 1000mL of 1,2, 4-trimethylbenzene uniformly in a container, and carrying out reduced pressure distillation at 80-125 ℃ and 40-10 kPa. When the system distillation raffinate is less than 1000mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.5%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of ethanol is gradually added under the stirring condition, the reaction is carried out for 2 hours at 78 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with 13.8 weight percent of chlorine is obtained after the reaction is finished. The alcoholysis product is subjected to repeated 2 times of normal pressure distillation at 78 ℃ until the ethanol is substantially completely distilled off, and 120mL of ethanol is used for redissolving after the distillation is finished. Then filtering and separating to obtain the organic waste liquid with chlorine content of 5.3wt% and a small amount of solid waste. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 7
500mL of the titanium-containing waste liquid and 500mL of 1,2, 3-trimethylbenzene are uniformly mixed in a container, and atmospheric distillation is carried out at 110-185 ℃. When the system distillation raffinate is less than 500mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.8%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of ethanol is gradually added under the stirring condition, the reaction is carried out for 2 hours at 78 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with 13.8 weight percent of chlorine is obtained after the reaction is finished. The alcoholysis product was distilled under normal pressure at a temperature of 78℃until substantially all of the ethanol was distilled off, and after the completion of the distillation, the resultant was redissolved in 120mL of ethanol to obtain a liquid mixture having a chlorine content of 7.1 wt%. And (3) carrying out neutralization reaction on the liquid mixture and a proper amount of sodium hydroxide solid, reacting at 78 ℃ until the solution is neutral, and then carrying out filter pressing separation to obtain the organic waste liquid and white solid waste residue with the chlorine content of 0.3 wt%. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 8
Mixing 500mL of titaniferous waste liquid and 1000mL of 1,3, 5-trimethylbenzene uniformly in a container, and carrying out reduced pressure distillation at 80-125 ℃ and 40-10 kPa. When the system distillation raffinate is less than 1000mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.2%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of ethanol is gradually added under the stirring condition, the reaction is carried out for 2 hours at 78 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with 13.8 weight percent of chlorine is obtained after the reaction is finished. The above alcoholysis product was subjected to repeated 2 times of atmospheric distillation at 78℃until substantially all of the ethanol was distilled off, and after the completion of each distillation, 120mL of ethanol was redissolved to obtain a liquid mixture having a chlorine content of 5.3% by weight. And (3) carrying out neutralization reaction on the liquid mixture and a proper amount of sodium hydroxide solid, reacting at 78 ℃ until the solution is neutral, and then carrying out filter pressing separation to obtain the organic waste liquid and white solid waste residue with the chlorine content of 0.3 wt%. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 9
500mL of titanium-containing waste liquid and 500mL of propylbenzene are uniformly mixed in a container, and atmospheric distillation is carried out at 110-185 ℃. When the system distillation raffinate is less than 500mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 83.8%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 100mL of methanol is gradually added under the stirring condition for reaction for 2h at 64 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with the chlorine content of 16.5wt% is obtained after the reaction is finished. And (3) carrying out normal pressure distillation on the alcoholysis product for 1 time, wherein the distillation temperature is 64 ℃, distilling until the methanol is basically completely distilled, redissolving the alcoholysis product with 100mL of methanol after the distillation is finished, and then filtering and separating to obtain an organic waste liquid with the chlorine content of 8.3wt% and a small amount of solid waste residues. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 10
Mixing 500mL of titaniferous waste liquid and 1000mL of 1,2, 4-trimethylbenzene uniformly in a container, and carrying out reduced pressure distillation at 80-125 ℃ and 40-10 kPa. When the system distillation raffinate is less than 1000mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.6%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of methanol is gradually added under the stirring condition to react for 2h at 64 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and a pale yellow alcoholysis product with the chlorine content of 14.8wt% is obtained after the reaction is finished. The alcoholysis product was subjected to repeated 2 times of atmospheric distillation at a distillation temperature of 64℃until substantially all of the methanol was distilled off, and after completion of each distillation, 120mL of methanol was redissolved. Then filtering and separating to obtain the organic waste liquid with the chlorine content of 6.8wt% and a small amount of solid waste. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 11
500mL of the titanium-containing waste liquid and 500mL of 1,2, 3-trimethylbenzene are uniformly mixed in a container, and atmospheric distillation is carried out at 110-185 ℃. When the system distillation raffinate is less than 500mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.5%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 100mL of methanol is gradually added under the stirring condition for reaction for 2h at 64 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and light yellow alcoholysis product with the chlorine content of 16.5wt% is obtained after the reaction is finished. The alcoholysis product was distilled under normal pressure at a temperature of 64℃until substantially all of the methanol was distilled off, and after completion of the distillation, it was redissolved with 100mL of methanol to obtain a liquid mixture having a chlorine content of 8.3 wt%. And (3) carrying out neutralization reaction on the liquid mixture and a proper amount of sodium hydroxide solid, reacting at 64 ℃ until the solution is neutral, and then carrying out filter pressing separation to obtain the organic waste liquid and white solid waste residue with the chlorine content of 0.3 wt%. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 12
Mixing 500mL of titaniferous waste liquid and 1000mL of 1,3, 5-trimethylbenzene uniformly in a container, and carrying out reduced pressure distillation at 80-125 ℃ and 40-10 kPa. When the system distillation raffinate is less than 1000mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.2%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of methanol is gradually added under the stirring condition to react for 2h at 64 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and a pale yellow alcoholysis product with the chlorine content of 14.8wt% is obtained after the reaction is finished. The above alcoholysis product was subjected to repeated 2 times of atmospheric distillation at a distillation temperature of 64℃until substantially all of the methanol was distilled off, and after the completion of each distillation, 120mL of methanol was redissolved to obtain a liquid mixture having a chlorine content of 6.8% by weight. And (3) carrying out neutralization reaction on the liquid mixture and a proper amount of sodium hydroxide solid, reacting at 64 ℃ until the solution is neutral, and then carrying out filter pressing separation to obtain the organic waste liquid and white solid waste residue with the chlorine content of 0.3 wt%. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 13
500mL of titanium-containing waste liquid and 500mL of propylbenzene are uniformly mixed in a container, and atmospheric distillation is carried out at 110-185 ℃. When the system distillation raffinate is less than 500mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 83.8%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of ethanol is gradually added under the stirring condition, the reaction is carried out for 2 hours at 78 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and after the reaction is finished, light yellow alcoholysis product with the chlorine content of 12.9wt%. And (3) carrying out normal pressure distillation on the alcoholysis product for 1 time, wherein the distillation temperature is 78 ℃, distilling until the ethanol is basically completely distilled, redissolving the alcoholysis product with 120mL of ethanol after the distillation is finished, and then filtering and separating to obtain an organic waste liquid with the chlorine content of 6.2wt% and a small amount of solid waste residues. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 14
Mixing 500mL of titaniferous waste liquid and 1000mL of 1,2, 4-trimethylbenzene uniformly in a container, and carrying out reduced pressure distillation at 80-125 ℃ and 40-10 kPa. When the system distillation raffinate is less than 1000mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.6%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of ethanol is gradually added under the stirring condition, the reaction is carried out for 2 hours at 78 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and after the reaction is finished, light yellow alcoholysis product with the chlorine content of 12.9wt%. The alcoholysis product is subjected to repeated 2 times of normal pressure distillation at 78 ℃ until the ethanol is substantially completely distilled off, and 120mL of ethanol is used for redissolving after the distillation is finished. Then filtering and separating to obtain the organic waste liquid with chlorine content of 4.8wt% and a small amount of solid waste. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 15
500mL of the titanium-containing waste liquid and 500mL of 1,2, 3-trimethylbenzene are uniformly mixed in a container, and atmospheric distillation is carried out at 110-185 ℃. When the system distillation raffinate is less than 500mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.5%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of ethanol is gradually added under the stirring condition, the reaction is carried out for 2 hours at 78 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and after the reaction is finished, light yellow alcoholysis product with the chlorine content of 12.9wt%. The alcoholysis product was distilled under normal pressure at a temperature of 78℃until substantially all of the ethanol was distilled off, and after the completion of the distillation, the resultant was redissolved in 120mL of ethanol to obtain a liquid mixture having a chlorine content of 6.2 wt%. And (3) carrying out neutralization reaction on the liquid mixture and a proper amount of sodium hydroxide solid, reacting at 78 ℃ until the solution is neutral, and then carrying out filter pressing separation to obtain the organic waste liquid and white solid waste residue with the chlorine content of 0.3 wt%. And (3) burning the organic waste liquid, and burying the solid waste residue.
Example 16
Mixing 500mL of titaniferous waste liquid and 1000mL of 1,3, 5-trimethylbenzene uniformly in a container, and carrying out reduced pressure distillation at 80-125 ℃ and 40-10 kPa. When the system distillation raffinate is less than 1000mL, the distillation is stopped, and the distillation raffinate still has obvious fluidity after cooling. The recovery rate of titanium tetrachloride was 84.2%.
30mL of the distillation residual liquid is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 120mL of ethanol is gradually added under the stirring condition, the reaction is carried out for 2 hours at 78 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and after the reaction is finished, light yellow alcoholysis product with the chlorine content of 12.9wt%. The above alcoholysis product was subjected to repeated 2 times of atmospheric distillation at 78℃until substantially all of the ethanol was distilled off, and after the completion of each distillation, 120mL of ethanol was redissolved to obtain a liquid mixture having a chlorine content of 4.8% by weight. And (3) carrying out neutralization reaction on the liquid mixture and a proper amount of sodium hydroxide solid, reacting at 78 ℃ until the solution is neutral, and then carrying out filter pressing separation to obtain the organic waste liquid and white solid waste residue with the chlorine content of 0.3 wt%. And (3) burning the organic waste liquid, and burying the solid waste residue.
Comparative example 1
500mL of titanium-containing waste liquid is distilled at the temperature of 110-185 ℃ under normal pressure, the reaction system gradually becomes viscous along with the distillation, the distillation is stopped, the fluidity of the distilled residual liquid is poor after cooling, and scaling and blockage are easy to occur. The recovery rate of titanium tetrachloride was 50.4%.
60mL of water is added into a 300mL glass reaction kettle with mechanical stirring, a reflux condenser pipe and nitrogen protection, 30mL of the distillation residual liquid is gradually added under the stirring condition, the reaction temperature is maintained to be lower than 100 ℃, HCl generated in the reaction process is discharged through tail gas and then is neutralized and absorbed, and an oil, water and solid three-phase mixture is obtained after the reaction is finished. Because of the water and HCl, the mixture is acidic and difficult to incinerate. Particularly under the increasingly stringent environmental requirements, the mixtures are difficult to handle in the catalyst production area, but are transported to remote areas, which results in complex and costly subsequent treatment processes and adverse environmental protection.
As can be seen from comparison of examples and comparative examples, compared with the currently adopted method, the method provided by the invention is simpler and more practical, avoids scaling and blocking tendency in the distillation process of the existing method, and improves the recovery rate of titanium tetrachloride in the titanium-containing waste liquid, and the used high-boiling point solvent does not have adverse effect on the preparation of the catalyst, so that the integral distillation operation is easier to implement, and the related running cost is reduced; in addition, the method greatly reduces the waste water and waste residue generated in the treatment process, greatly reduces the chlorine content in the obtained organic waste liquid, can directly burn the organic waste liquid, and has obvious environmental protection and economic benefits. In addition, the method of the present invention can be conveniently applied to existing catalyst production systems.
The foregoing description of embodiments of the invention has been presented for purposes of illustration and description, and is not intended to be exhaustive or limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the various embodiments described.
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
Claims (25)
1. A method for treating a titanium-containing waste liquid, which is a titanium tetrachloride-containing waste liquid produced in a process for producing a titanium-based polyolefin catalyst, comprising the steps of:
(1) Contacting the titanium-containing waste liquid with at least one aromatic hydrocarbon to obtain a mixture, wherein the aromatic hydrocarbon has a general formula of C n H 2n-6 ，20≥n≥7；
(2) Distilling the mixture obtained in the step (1) in a distillation device, wherein the top of the distillation device is separated to obtain a titanium tetrachloride-containing material, and the bottom of the distillation device is obtained to obtain distillation raffinate;
(3) Mixing the distillation residual liquid obtained in the step (2) with an alcohol compound for alcoholysis reaction to obtain an alcoholysis product containing hydrogen chloride;
(4) Distilling the alcoholysis product obtained in the step (3) to remove hydrogen chloride in the alcoholysis product and obtain an alcoholysis product with reduced chlorine content;
(5) Directly carrying out solid-liquid separation on the alcoholysis product with reduced chlorine content obtained in the step (4), or carrying out neutralization reaction on the alcoholysis product with reduced chlorine content and an alkaline substance, and then carrying out solid-liquid separation to obtain organic waste liquid and solid waste residue;
wherein the boiling point of the aromatic hydrocarbon is 150-179 ℃.
2. The method for treating a titanium-containing waste liquid according to claim 1, wherein the aromatic hydrocarbon has a general formula of C n H 2n-6 ，12≥n≥8。
3. The method for treating a titanium-containing waste liquid according to claim 1, wherein the aromatic hydrocarbon is at least one selected from the group consisting of o-xylene, m-xylene, p-xylene, o-diethylbenzene, m-diethylbenzene, p-diethylbenzene, propylbenzene, isopropylbenzene, 1,2, 4-trimethylbenzene, 1,2, 3-trimethylbenzene, 1,3, 5-trimethylbenzene, p-methylisopropylbenzene, 1,2,3, 5-tetramethylbenzene, butylbenzene, sec-butylbenzene, tert-butylbenzene, isobutylbenzene, methylisobutylbenzene, pentylbenzene, and tert-pentylbenzene.
4. The method for treating a titanium-containing waste liquid according to claim 3, wherein the aromatic hydrocarbon is at least one selected from the group consisting of propylbenzene, isopropylbenzene, 1,2, 4-trimethylbenzene, 1,2, 3-trimethylbenzene, 1,3, 5-trimethylbenzene, p-methylisopropylbenzene, sec-butylbenzene, tert-butylbenzene, isobutylbenzene and methylisobutylketone.
5. The method for treating a titanium-containing waste liquid according to claim 1, wherein a volume ratio of the aromatic hydrocarbon to the titanium-containing waste liquid is 0.05 to 5.0:1.
6. the method for treating a titanium-containing waste liquid according to claim 5, wherein a volume ratio of the aromatic hydrocarbon to the titanium-containing waste liquid is 0.1 to 2.0:1.
7. the method for treating a titanium-containing waste liquid according to claim 1, wherein in the step (2), the titanium tetrachloride-containing material separated from the top of the distillation apparatus is fed into a rectifying tower to rectify and recover titanium tetrachloride.
8. The method for treating a titanium-containing waste liquid according to claim 1, wherein the alcohol compound is at least one of a monohydric alcohol, a dihydric alcohol and a polyhydric alcohol.
9. The method for treating a titanium-containing waste liquid according to claim 8, wherein the monohydric alcohol is at least one of alcohol compounds represented by the general formula ROH, wherein R is C 1 -C 12 Straight-chain or branched alkyl, C 3 -C 12 Cycloalkyl or C of (C) 7 -C 12 An aralkyl group of (a).
10. The method for treating a titanium-containing waste liquid according to claim 9, wherein the monohydric alcohol is at least one of methanol, ethanol, n-propanol, isopropanol, n-butanol, isobutanol, sec-butanol, tert-butanol, n-pentanol, n-hexanol, n-heptanol, n-octanol, n-nonanol, n-decanol, cyclopentanol, benzyl alcohol, and phenethyl alcohol.
11. The method for treating a titanium-containing waste liquid according to claim 8, wherein the dihydric alcohol is C 2 -C 12 Is a diol of (3).
12. The method for treating a titanium-containing waste liquid according to claim 11, wherein the dihydric alcohol is ethylene glycol and/or propylene glycol.
13. The method for treating a titanium-containing waste liquid according to claim 8, wherein the polyhydric alcohol is C 2 -C 12 Is a triol of (c).
14. The method for treating a titanium-containing waste liquid according to claim 13, wherein the polyhydric alcohol is glycerol.
15. The method for treating a titanium-containing waste liquid according to claim 1, wherein in the step (3), the volume ratio of the alcohol compound to the distillation raffinate is 0.05 to 15:1.
16. the method for treating a titanium-containing waste liquid according to claim 15, wherein in the step (3), the volume ratio of the alcohol compound to the distillation raffinate is 0.1 to 10:1.
17. The method for treating a titanium-containing waste liquid according to claim 16, wherein in the step (3), the volume ratio of the alcohol compound to the distillation raffinate is 0.2 to 5:1.
18. the method for treating a titanium-containing waste liquid according to claim 1, wherein in the step (3), the alcoholysis reaction is performed under stirring, and the temperature of the alcoholysis reaction is not higher than the boiling point of the alcohol compound; the mode of mixing the distillation raffinate with the alcohol compound is as follows: adding an alcohol compound to the titanium-containing distillation raffinate or adding the titanium-containing distillation raffinate to the alcohol compound.
19. The method for treating a titanium-containing waste liquid according to claim 18, wherein the distillation raffinate is mixed with the alcohol compound in the following manner: alcohol compounds are added to the titanium-containing distillation raffinate.
20. The method for treating a titanium-containing waste liquid according to claim 1, wherein in the step (4), the distillation treatment is an atmospheric distillation treatment or a vacuum distillation treatment, the number of times of distillation is one or more, and the temperature of the distillation treatment is not lower than the initial boiling point of the alcoholysis product.
21. The method for treating a titanium-containing waste liquid according to claim 1, wherein the step (4) further comprises: after the distillation treatment, the alcohol compound or the distillation fraction is added to the distillation product.
22. The method for treating a titanium-containing waste liquid according to claim 1, wherein in the step (5), the alkaline substance is at least one selected from the group consisting of an alkali metal hydroxide, an alkali metal oxide, an alkaline earth metal hydroxide and an alkaline earth metal oxide.
23. The method for treating a titanium-containing waste liquid according to claim 22, wherein in the step (5), the alkaline substance is at least one selected from the group consisting of sodium hydroxide, potassium hydroxide, calcium hydroxide and calcium oxide.
24. The method for treating a titanium-containing waste liquid according to claim 1, wherein the titanium-containing waste liquid is a catalyst mother liquid produced in a process of producing a titanium-based polyolefin catalyst or a raffinate containing titanium tetrachloride and a high-boiling substance obtained by distilling a part of titanium tetrachloride from a catalyst mother liquid produced in a process of producing a titanium-based polyolefin catalyst.
25. The method for treating a titanium-containing waste liquid according to any one of claims 1 to 24, wherein the organic waste liquid is directly subjected to incineration treatment, and the solid waste is treated as solid waste.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911025535.3A CN112707561B (en) | 2019-10-25 | 2019-10-25 | Treatment method of titanium-containing waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911025535.3A CN112707561B (en) | 2019-10-25 | 2019-10-25 | Treatment method of titanium-containing waste liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112707561A CN112707561A (en) | 2021-04-27 |
| CN112707561B true CN112707561B (en) | 2023-05-12 |
Family
ID=75540870
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911025535.3A Active CN112707561B (en) | 2019-10-25 | 2019-10-25 | Treatment method of titanium-containing waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112707561B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7935651B1 (en) * | 2010-02-04 | 2011-05-03 | Equistar Chemicals, L.P. | Method for preparing a Ziegler-Natta catalyst |
| CN103044257A (en) * | 2012-12-29 | 2013-04-17 | 南京化工职业技术学院 | Alcoholysis method and device system for producing dioctyl terephthalate by polyester wastes |
| CN104556219A (en) * | 2013-10-29 | 2015-04-29 | 中国石油化工股份有限公司 | Method for preparing nano-TiO2 |
| CN109415223A (en) * | 2016-08-03 | 2019-03-01 | 科莱恩国际有限公司 | From the method for devil liquor recovery titanium (halogenated) alkoxide |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5242549A (en) * | 1991-12-06 | 1993-09-07 | Shell Oil Company | Distillation separation process of titanium tetrachloride and halohydrocarbon |
| CN1161318A (en) * | 1995-11-01 | 1997-10-08 | 联合碳化化学品及塑料技术公司 | Method for removal of metal (Ti or V) alkoxide compounds from liquid hydrocarbon |
| CN1078565C (en) * | 1999-01-22 | 2002-01-30 | 清华大学 | Method for preparing nano sized titanium dioxide powder by alcoholysis from titanic chloride |
| EP2452920A1 (en) * | 2010-11-12 | 2012-05-16 | Borealis AG | A method for recovering transition metal tetrahalide and hydrocarbons from a waste stream |
| CN103420437B (en) * | 2012-05-17 | 2015-10-07 | 中国石油化工股份有限公司 | A kind of recovery and treatment method of titaniferous waste liquid |
-
2019
- 2019-10-25 CN CN201911025535.3A patent/CN112707561B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7935651B1 (en) * | 2010-02-04 | 2011-05-03 | Equistar Chemicals, L.P. | Method for preparing a Ziegler-Natta catalyst |
| CN103044257A (en) * | 2012-12-29 | 2013-04-17 | 南京化工职业技术学院 | Alcoholysis method and device system for producing dioctyl terephthalate by polyester wastes |
| CN104556219A (en) * | 2013-10-29 | 2015-04-29 | 中国石油化工股份有限公司 | Method for preparing nano-TiO2 |
| CN109415223A (en) * | 2016-08-03 | 2019-03-01 | 科莱恩国际有限公司 | From the method for devil liquor recovery titanium (halogenated) alkoxide |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112707561A (en) | 2021-04-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102336432B (en) | Separation method for recovering olefin polymerization catalyst mother liquid | |
| CN102229586B (en) | Preparation method for alpha-acetyl-gamma-butyrolactone | |
| CN103030232A (en) | Method for treating titanium-containing waste liquid produced by polyolefin catalyst | |
| CN102105432B (en) | Method for recovering (meth)acrylic acid ester | |
| CN1639067B (en) | Treatment of a titanium tetrachloride-containing waste stream | |
| CN103420413A (en) | Method of recycling refined titanium tetrachloride from titanium-containing waste liquid | |
| CN112707437A (en) | Treatment method of titanium tetrachloride-containing waste liquid | |
| CN112707561B (en) | Treatment method of titanium-containing waste liquid | |
| CN105452230A (en) | Process for the manufacture of epoxy-monomers and epoxides | |
| CN112707557B (en) | Treatment method of titanium-containing waste liquid | |
| CN112707560B (en) | Treatment method of titanium-containing waste liquid, titanium dioxide raw material and application | |
| CN102858727B (en) | Process for production of alkylene carbonates and/or alkylene glycols | |
| CN112707435A (en) | Method for recovering refined titanium tetrachloride from titanium tetrachloride-containing waste liquid | |
| CN112707436B (en) | Treatment method of titanium tetrachloride-containing waste liquid | |
| CN112707559B (en) | Treatment method of titanium-containing distillation raffinate | |
| CN112707532B (en) | Treatment method of titanium-containing distillation residual liquid, titanium white raw material and application | |
| CN112707530B (en) | Treatment method of titanium-containing distillation residual liquid | |
| CN114426306B (en) | Titanium polyolefin catalyst mother liquor treatment device and method | |
| CN112707556A (en) | Titanium-containing waste liquid treatment method and titanium-containing dry powder | |
| CN112723580A (en) | Method for reducing chlorine content in chlorine-containing organic waste liquid and method for treating chlorine-containing organic waste liquid | |
| CN103028224A (en) | Method for treating titanium tetrachloride-containing waste liquid | |
| CN112708782B (en) | Titanium-containing waste liquid treatment method and titanium-containing dry powder | |
| CN112707449B (en) | Method for treating titanium-containing waste liquid | |
| CN112239226A (en) | Method for treating titanium-containing waste liquid generated in production process of polyolefin catalyst | |
| CN103772153A (en) | Synthesis method of 4-chloro-3-cresol and system thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |