CN1337432A - Production process and equipment for hydrogenated rosin and pinane with high cis-to-trans ratio - Google Patents
Production process and equipment for hydrogenated rosin and pinane with high cis-to-trans ratio Download PDFInfo
- Publication number
- CN1337432A CN1337432A CN 01128415 CN01128415A CN1337432A CN 1337432 A CN1337432 A CN 1337432A CN 01128415 CN01128415 CN 01128415 CN 01128415 A CN01128415 A CN 01128415A CN 1337432 A CN1337432 A CN 1337432A
- Authority
- CN
- China
- Prior art keywords
- pinane
- rosin
- staybelite
- high cis
- trans ratio
- 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.)
- Granted
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Catalysts (AREA)
Abstract
The method for preparing hydrogenated rosin and high cis-trans-pinane by using liquid pine oleoresin or rosin dissolved by 200# solvent naphtha as raw material, adopting skeletal nickel as catalyst and making them implement hydrogenation reaction is characterized by that its reaction temp. is 80-180 deg.C, hydrogen pressure is 1.0-6.0 MPa or it adopts Pd/c as catalyst, its reaction hydrogen pressure is 0.1-2.0 MPa, and its temp. is 130-180 deg.C. The invention adopts the non-noble metal nickel as catalyst so as to greatly reduce production cost of hydrogenated rosin, and its reaction condition is moderate, technological process is short, operation is easy, and the pinane cis-trans-ratio is 13-20.
Description
Technical field
The present invention relates to a kind of colophony processing method and equipment, the manufacture method and the equipment of particularly a kind of staybelite and pinane.
Background technology
The rosiny main component is the abietic type acid, is called for short " abietic acid ".Abietic acid has conjugated double bond, easily with atmosphere in the oxygen effect, make rosiny color burn, crisp, the grade decline of qualitative change.The method of employing shortening can change the double bond structure of abietic acid, makes its rock steady structure that is tending towards alicyclic ring, eliminates rosin and has the shortcoming that causes because of conjugated double bond.When one of abietic acid two key are saturated by hydrogen, be called the dihydroabietic acid, when two two keys all then are called tetrahydroabietic acid when saturated by hydrogen.Staybelite is to contain the dihydroabietic acid, and tetrahydrochysene rosin is to contain tetrahydroabietic acid.Staybelite has characteristics such as antioxidant property is good, fragility is little, thermostability is high, lighter color, can be widely used for aspects such as tackiness agent, soldering flux, printing ink, paint, papermaking, rubber.Terebinthine main component is a firpene, and firpene makes pinane through shortening, and pinane has cis and trans two kinds of isomerss.Because trans pinane C2-H key is subjected to the dimethylated protection of four carbocyclic ring upper eye lids; sterically hindered increase; compare with cis-pinane that the tertiary hydrogen reactive behavior is relative on the C2 position reduces; and the active corresponding increase of parahydrogen on the C3, C4 position; so can generate by products such as loose baras camphor and pinanol in the oxidizing reaction of making baras camphor, therefore the height along inverse ratio is the important control index that pinane is produced.And because cis, trans pinane are steric isomers, and the boiling point of the two only differs 1 ℃, can't carry out conventional rectification and purify, can only control by catalytic hydrogenation reaction, thereby how to improve along inverse ratio be the key of pinane production technology.
The following method of the general employing of the manufacturing of staybelite and pinane: rosin obtains rosin and turps through steam distillation, rosin is under molten state, with Pd/c is that catalyzer carries out hydrogenation reaction, and temperature of reaction is 220～270 ℃, and hydrogen pressure is 10～30MPa, reaction conditions is comparatively harsh, facility investment is big, and when temperature of reaction was higher than 250 ℃, abietic acid decarboxylation side reaction was serious, even part rosin generation cracking becomes rosinol, causes unstable product quality.The manufacture method of pinane is the firpene that earlier the turps rectifying separation is obtained more than 95%, and firpene obtains pinane through shortening again, and suitable inverse ratio is only between 9～11.And firpene easy generation temperature runaway in hydrogenation reaction, thereby cause generating by product to alkane in the Meng.As seen, there is long flow path in the whole production technology of staybelite and pinane, efficient is low, shortcomings such as process cost height, and the production of staybelite also needs to make catalyzer with precious metal palladium, and along with the development of society, the price of precious metal constantly rises, the price of palladium goes up at double in recent years, causes production cost constantly to increase.Production about staybelite has following patent application CN1097448A and CN1245192A at present, and the former adopts but crystallization decoloring method of fat liquid cooling, is catalyzer with Pd/c, 130～180 ℃ of temperature, carries out hydrogenation reaction under hydrogen pressure 3.0～8.0MPa; The latter also is to be catalyzer with Pd/c, adopts the fixed bed continuous hydrogenation, and temperature of reaction is 180～260 ℃, and hydrogen pressure is 10～20MPa, but the temperature and pressure that this method need be reacted is all higher, the equipment complexity, and production cost is also higher.
Technology contents
The inventor after deliberation and explore has found the method for preparing staybelite and pinane with high cis-to-trans ratio under the condition of low-temp low-pressure, and particular content is as follows:
With rosin is raw material, under the effect of catalyzer, the compressive reaction that in hydrogenator, heats up, product is after filtration, underpressure distillation obtains staybelite and pinane with high cis-to-trans ratio, perhaps is raw material with the dissolving rosin, make staybelite, be raw material system pinane with high cis-to-trans ratio with turps perhaps, be characterized in: the catalyzer of employing is base metal skeleton nickel (Raney's nickel Nanny-Ni), and temperature of reaction is 80～180 ℃, pressure is 3.0～6.0Mpa, and the time is 1.5～2.5 hours.Adopt present method to obtain superfine staybelite and reach 13～20 pinane along inverse ratio through underpressure distillation.
The manufacture method of staybelite recited above and pinane with high cis-to-trans ratio, except turps and rosin, rosin must could react in liquid phase with dissolution with solvents earlier, the solvent that dissolving rosin adopted is turps or 200# solvent oil (alkane of distillation oil), and dissolving rosin of the present invention is that turps or 200# solvent oil and rosin are made into 35～60% solution.
The consumption of skeletal nickel catalyst recited above is the total weight that adds according to rosin or turps, rosin, and catalyzer accounts for 3～10% of total charging capacity.
The inventor also finds, under the condition of low-temp low-pressure, with rosin is raw material, the 200# solvent oil is a solvent, the Pd/c that contains palladium 5% is a catalyzer, in the autoclave that the static seal magnetic stirring apparatus is housed under 130～178 ℃ of the control hydrogen pressure 0.1～2.0MPa, temperature, also can make the high-quality staybelite, the employing fixed bed continuous hydrogenation of being introduced in it and the existing patent documentation, temperature of reaction is 180～260 ℃, and hydrogen pressure is that the prepared staybelite quality of 10～20Mpa is identical.
Major advantage of the present invention is that the technological process of production is short, equipment is few, and the products obtained therefrom staybelite is of light color, the suitable inverse ratio height of pinane, and key is to adopt base metal nickel to make catalyzer, and adopt the autoclave that the static seal magnetic stirring apparatus is housed, greatly reduce production cost; If need not produce pinane, can rosin be raw material also, add the 200# solvent oil of an amount of ratio, under the effect of skeletal nickel catalyst, carry out hydrogenation reaction, produce staybelite separately; Be raw material with turps perhaps, under the effect of skeletal nickel catalyst, produce pinane with high cis-to-trans ratio separately, this shows that production method of the present invention is flexible and changeable.Can also rosin be raw material in addition, No. 200 oil be solvent, and employing Pd/c is a catalyzer, carries out hydrogenation reaction and produce staybelite under 130～180 ℃ of temperature, hydrogen pressure 0.1～2.0MPa.This method is because reaction pressure is low, and is less demanding to production unit, so construction investment is few, and the also corresponding decline of process cost is easy to apply.
Description of drawings
Accompanying drawing 1 is a process flow diagram of the present invention.
From Fig. 1, see, skeletal nickel catalyst joined in the autoclave 1, rosin from head tank 2 with certain speed Be added to autoclave 1, under the condition of 80～180 ℃ of temperature, hydrogen pressure 1.0～6.0Mpa, starting agitator, to carry out hydrogenation anti-Should, behind generation Foral and the pinane with high cis-to-trans ratio mixture, through hold-up vessel 3, filtrate is isolated the hydrogenation pine through decompression distillation Perfume (or spice) and hydroterpin, hydroterpin enters the rectifying column fractionation with the state of saturated vapor, and cat head obtains pinane with high cis-to-trans ratio, Tower reactor obtains heavy oil.
The structure of capital equipment autoclave is described as follows: adopt the static seal magnetic stirring apparatus, agitator is divided into 2 to 3 layers, the end Layer is anchor formula, turbine type or propeller agitator, in, the upper strata is turbine type or propeller agitator, be inserted with in the still into and out of Material pipe and probe tube.
Embodiment
Embodiment one:
Get the clean rosin liquid that contains turps 35～60%, add in the autoclave after metering by header tank, and add skeletal nickel catalysts by 3～10% of charging capacity, through vacuumizing, behind the air in the hydrogen exchange autoclave, regulating hydrogen pressure to 3.0 in the still～6.0MPa, start autoclave and stir and heating system, be warming up to 80～180 ℃, and constantly feed hydrogen, and to keep still straightening to the hydrogenation that sets and finish, the reaction times is 1.5～2.5 hours.Stopping autoclave stirring, allow catalyst precipitation after 5～10 minutes, emptying is to still internal pressure 0.3～1.0MPa, by the discharge nozzle in the insertion still material is pressed into strainer and removes the catalyzer of taking out of, filtrate is isolated staybelite and hydroterpin through underpressure distillation, hydroterpin enters the rectifying tower fractionation with the state of saturation steam, and cat head obtains pinane with high cis-to-trans ratio, and the tower still obtains heavy oil.The products obtained therefrom staybelite meets the superfine standard of standard GB/T14020-92, and pinane is 13～20 along inverse ratio.
When repeating to feed intake, should keep autoclave reinforced under positive pressure, avoid the air admission autoclave, so that omit operation stepss such as vacuumizing in the still, displacement.Catalyzer replenishes a little by about 2% of former input amount.
Embodiment two:
Get superfine or the one-level colophonium powder is broken to particle diameter less than 50mm, with 200# solvent oil heating for dissolving, be made into the solution of oil-containing 35～60%, and press 3～10% of rosin charging capacity and add skeletal nickel catalysts, under 80～180 ℃ of temperature, hydrogen pressure 3.0～6.0MPa, hydrogenation reaction 1.5～2.5 hours, after filtration, underpressure distillation obtains staybelite and 200# solvent oil.The product staybelite meets the superfine standard of standard GB/T14020-92, and the solvent oil circulating involuting system continues to use.
Embodiment three:
Get light oil and drop into autoclave after metering, and add skeletal nickel catalysts by 3～10% of charging capacity, 80～180 ℃ of temperature, under hydrogen pressure 1.0～6.0MPa, hydrogenation reaction 1.5～2.5 hours, after filtration, to obtain along inverse ratio be 13～20 pinane in rectification under vacuum, all the other detailed parts are embodiment one roughly the same.
Embodiment four:
Get superfine or the one-level colophonium powder is broken to particle diameter less than 50mm, with 200# solvent oil heating for dissolving, be made into the solution of oil-containing 35～60%, and add the Pd/c catalyzer contain palladium about 5% by 0.1～0.2% of rosin charging capacity, 130～178 ℃ of temperature, hydrogenation reaction is 1.5～2.5 hours under hydrogen pressure 0.1～2.0MPa, after filtration, underpressure distillation obtains staybelite and 200# solvent oil.The product staybelite meets the superfine standard of standard GB/T14020-92, and the solvent oil circulating involuting system continues to use.All the other not detailed parts are embodiment one roughly the same.
Claims (5)
1. the manufacture method of staybelite and pinane with high cis-to-trans ratio, with rosin, dissolving rosin, turps is raw material, under the effect of catalyzer, compressive reaction heats up in hydrogenator, product after filtration, underpressure distillation obtains staybelite and pinane with high cis-to-trans ratio, and it is characterized in that: the catalyzer of employing is the base metal skeleton nickel, and temperature of reaction is 80～180 ℃, pressure is 3.0～6.0Mpa, and the time is 1.5～2.5 hours.
2. the manufacture method of staybelite according to claim 1 and pinane with high cis-to-trans ratio is characterized in that dissolving rosin is 35～60% the solution that turps or 200# solvent oil and rosin are made into.
3. the manufacture method of staybelite according to claim 1 and pinane with high cis-to-trans ratio is characterized in that skeletal nickel catalyst adds by 3～10% of charging capacity.
4. the manufacture method of a staybelite is characterized in that with rosin being raw material, and the 200# solvent oil is a solvent, and the Pd/c that contains palladium 5% is a catalyzer, under 130～178 ℃ of hydrogen pressure 0.1～2.0MPa, temperature, and shortening hydrogen manufacturing rosin.
5. the equipment that uses of the manufacture method of staybelite as claimed in claim 1 and pinane with high cis-to-trans ratio, it is characterized in that hydrogenator is a static seal magnetic agitation autoclave, agitator is anchor formula, turbine type or push type, divides 1～3 layer, is inserted with charging and discharging pipe and stopple coupon in the still.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011284153A CN1185317C (en) | 2001-09-03 | 2001-09-03 | Production process and equipment for hydrogenated rosin and pinane with high cis-to-trans ratio |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011284153A CN1185317C (en) | 2001-09-03 | 2001-09-03 | Production process and equipment for hydrogenated rosin and pinane with high cis-to-trans ratio |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1337432A true CN1337432A (en) | 2002-02-27 |
| CN1185317C CN1185317C (en) | 2005-01-19 |
Family
ID=4668274
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011284153A Expired - Fee Related CN1185317C (en) | 2001-09-03 | 2001-09-03 | Production process and equipment for hydrogenated rosin and pinane with high cis-to-trans ratio |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1185317C (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1317347C (en) * | 2004-09-27 | 2007-05-23 | 广西大学 | Water-white hydrogenating rosin production |
| CN106281039A (en) * | 2015-06-08 | 2017-01-04 | 中国石油化工股份有限公司 | The preparation method of crude sulfate turpentine Hydrobon catalyst and hydrofining technology |
| CN106905855A (en) * | 2017-03-29 | 2017-06-30 | 南宁市青秀区嘉利林化有限公司 | The method that hydrogenated rosin is prepared from rosin |
| ES2647235R1 (en) * | 2014-10-15 | 2018-02-02 | Resinas Brasil Industria E Comercio Ltda | Process for obtaining hydrogenated resin rubber and products obtained through it |
| CN109321269A (en) * | 2018-09-12 | 2019-02-12 | 广西大学 | The method that pine tree effluent cracked-hydrogenate simultaneously preparation bio oil and monoterpene alkane |
| CN114073916A (en) * | 2020-08-18 | 2022-02-22 | 中石化南京化工研究院有限公司 | Method for feeding reactants in pressure reactor |
-
2001
- 2001-09-03 CN CNB011284153A patent/CN1185317C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1317347C (en) * | 2004-09-27 | 2007-05-23 | 广西大学 | Water-white hydrogenating rosin production |
| ES2647235R1 (en) * | 2014-10-15 | 2018-02-02 | Resinas Brasil Industria E Comercio Ltda | Process for obtaining hydrogenated resin rubber and products obtained through it |
| CN106281039A (en) * | 2015-06-08 | 2017-01-04 | 中国石油化工股份有限公司 | The preparation method of crude sulfate turpentine Hydrobon catalyst and hydrofining technology |
| CN106281039B (en) * | 2015-06-08 | 2019-06-04 | 中国石油化工股份有限公司 | The preparation method and hydrofining technology of crude sulfate turpentine Hydrobon catalyst |
| CN106905855A (en) * | 2017-03-29 | 2017-06-30 | 南宁市青秀区嘉利林化有限公司 | The method that hydrogenated rosin is prepared from rosin |
| CN109321269A (en) * | 2018-09-12 | 2019-02-12 | 广西大学 | The method that pine tree effluent cracked-hydrogenate simultaneously preparation bio oil and monoterpene alkane |
| CN114073916A (en) * | 2020-08-18 | 2022-02-22 | 中石化南京化工研究院有限公司 | Method for feeding reactants in pressure reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1185317C (en) | 2005-01-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106008819B (en) | A kind of process units and production method of the low hydrogenated petroleum resin of colourity carbon nine | |
| CN1035012C (en) | Method for producing disproportionated rosin by using pine gum as raw material | |
| CN102351627A (en) | Process method for extracting normal hexane and isohexane from crude hexane | |
| EP0223035A1 (en) | Use of modified Raney catalysts in the production of aromatic diamino compounds | |
| CN102070988B (en) | Method for producing water-white hydrogenated rosin | |
| CN102872863B (en) | Carrier type catalyst and application of carrier type catalyst in low-pressure rosin hydrogenation | |
| CN1185317C (en) | Production process and equipment for hydrogenated rosin and pinane with high cis-to-trans ratio | |
| CN110229042A (en) | A kind of preparation method of high-purity n-hexane | |
| CN105646786A (en) | Method for preparing dicyclopentadiene hydrogenated petroleum resin from dicyclopentadiene directly | |
| CN106008820B (en) | Low colourity light dydrocarbon carbon nine is copolymerized the production system and method for hydrogenation resin | |
| CN109456793B (en) | Synchronous industrial co-production method | |
| CN101724450A (en) | Method for modifying heavy oil | |
| WO2016184328A1 (en) | Metal complex catalyst, preparation method thereof, and use thereof in preparing d,l-menthol | |
| CN102212314A (en) | Method for preparing water-white highly-hydrogenated rosin | |
| CN102344751A (en) | Method for simultaneously preparing terpene rosin resin and polymerized rosin from rosin as raw material | |
| CN113735677B (en) | Method for preparing cis-pinane by catalyzing alpha-pinene hydrogenation through L-malic acid intercalated magnesium-aluminum hydrotalcite supported ruthenium catalyst | |
| CN1089353C (en) | Process for preparing hydrogenated rosin | |
| CN114230453A (en) | Production method for synthesizing propionic acid by one-step hydrogenation | |
| WO2002072508A1 (en) | HYDROGENATION OF α-PINENE | |
| CN105315156B (en) | The synthetic method of 2 methylcyclohexyl acetates | |
| CN110511107A (en) | A method of polytypic n-hexane is produced using C5 oil is reformed | |
| CN107935845B (en) | Method for preparing cyclohexyl acetate by reactive distillation | |
| CN105669371A (en) | Production method of trimethylolethane | |
| JP3579507B2 (en) | Continuous production of cyclohexene by partial hydrogenation of benzene. | |
| CN117843598A (en) | Preparation method of methyl hexahydrophthalic anhydride |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20050119 Termination date: 20110903 |