CN111170853B - Production process and system for preparing cyclohexane plasticizer by liquid phase hydrogenation of o-benzene plasticizer - Google Patents
Production process and system for preparing cyclohexane plasticizer by liquid phase hydrogenation of o-benzene plasticizer Download PDFInfo
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- CN111170853B CN111170853B CN202010164770.5A CN202010164770A CN111170853B CN 111170853 B CN111170853 B CN 111170853B CN 202010164770 A CN202010164770 A CN 202010164770A CN 111170853 B CN111170853 B CN 111170853B
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- 239000004014 plasticizer Substances 0.000 title claims abstract description 54
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 21
- 239000007791 liquid phase Substances 0.000 title claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- UHOVQNZJYSORNB-UHFFFAOYSA-N benzene Substances C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 16
- 238000004821 distillation Methods 0.000 claims abstract description 50
- 239000011261 inert gas Substances 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims description 17
- XNGIFLGASWRNHJ-UHFFFAOYSA-N phthalic acid Chemical compound OC(=O)C1=CC=CC=C1C(O)=O XNGIFLGASWRNHJ-UHFFFAOYSA-N 0.000 claims description 3
- 239000000047 product Substances 0.000 abstract description 27
- 238000000926 separation method Methods 0.000 abstract description 20
- 239000006227 byproduct Substances 0.000 abstract description 6
- 238000010438 heat treatment Methods 0.000 abstract description 6
- 238000000034 method Methods 0.000 abstract description 5
- 238000002156 mixing Methods 0.000 abstract description 4
- 238000000746 purification Methods 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 230000000630 rising effect Effects 0.000 abstract description 3
- 230000005540 biological transmission Effects 0.000 abstract description 2
- 238000005243 fluidization Methods 0.000 abstract description 2
- 238000000605 extraction Methods 0.000 description 17
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 description 16
- 230000008929 regeneration Effects 0.000 description 12
- 238000011069 regeneration method Methods 0.000 description 12
- 239000002904 solvent Substances 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 238000005292 vacuum distillation Methods 0.000 description 6
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 description 4
- XTVRLCUJHGUXCP-UHFFFAOYSA-N 3-methyleneheptane Chemical compound CCCCC(=C)CC XTVRLCUJHGUXCP-UHFFFAOYSA-N 0.000 description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- LAIUFBWHERIJIH-UHFFFAOYSA-N 3-Methylheptane Chemical compound CCCCC(C)CC LAIUFBWHERIJIH-UHFFFAOYSA-N 0.000 description 2
- 239000005711 Benzoic acid Substances 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 235000010233 benzoic acid Nutrition 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 229920000915 polyvinyl chloride Polymers 0.000 description 2
- 239000004800 polyvinyl chloride Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- YIWUKEYIRIRTPP-UHFFFAOYSA-N 2-ethylhexan-1-ol Chemical compound CCCCC(CC)CO YIWUKEYIRIRTPP-UHFFFAOYSA-N 0.000 description 1
- UADWUILHKRXHMM-UHFFFAOYSA-N 2-ethylhexyl benzoate Chemical compound CCCCC(CC)COC(=O)C1=CC=CC=C1 UADWUILHKRXHMM-UHFFFAOYSA-N 0.000 description 1
- 206010007269 Carcinogenicity Diseases 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 description 1
- 230000007670 carcinogenicity Effects 0.000 description 1
- 231100000260 carcinogenicity Toxicity 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- -1 phthalic acid ester Chemical class 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 239000003566 sealing material Substances 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/30—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group
- C07C67/303—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group by hydrogenation of unsaturated carbon-to-carbon bonds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C67/54—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a production process and a system for preparing cyclohexane plasticizer by liquid phase hydrogenation of o-benzene plasticizer. The production process of cyclohexane plasticizer by liquid phase hydrogenation of o-benzene plasticizer includes the following steps: 1) introducing heated inert gas to the bottom of the reduced pressure distillation tower in a pulse pneumatic transmission mode; 2) and the plasticizer product enters the bottom of the reduced pressure distillation tower after being preheated, and the inlet of the plasticizer product on the reduced pressure distillation tower is higher than the inlet of the inert gas, so that the plasticizer product is mixed and heated with the rising inert gas flow in the downward flowing process, and the target product and the by-product are separated. The process and the system of the invention adopt a pulse mode to send heated inert gas to the reduced pressure distillation tower, and utilize the characteristic of large time and small time of the inert gas to better simulate fluidization mixing heating at the bottom of the reduced pressure distillation tower, thereby realizing better mixing heating and separation purification effects on the plasticizer product.
Description
Technical Field
The invention relates to the field of preparation of cyclohexane plasticizers by liquid phase hydrogenation of o-benzene plasticizers, in particular to a production process and a system for preparing cyclohexane plasticizers by liquid phase hydrogenation of o-benzene plasticizers.
Background
At present, the plasticizer is the largest additive variety in the modern plastic industry, plays a decisive role in promoting the development of the plastic industry, particularly the polyvinyl chloride PVC industry, and has wide application in the fields of synthetic rubber, paint, adhesive, sealing material and the like. Researches show that the traditional production device for preparing the plasticizer has the advantages of long reaction time, high energy consumption, low yield per unit time, unstable product quality, high water content and high acid value of a product detection result. And the prepared o-benzene plasticizer has toxicity and carcinogenicity.
In the process of preparing the cyclohexane plasticizer by liquid phase hydrogenation of the phthalic plasticizer, phthalic acid ester can generate benzoic acid monoester and corresponding alcohol or olefin through intramolecular elimination reaction at higher temperature, DOP can be decomposed into phthalic anhydride, 2-ethylhexyl alcohol and 2-ethyl hexene by heating, the olefin can be further changed into alkane under hydrogen atmosphere, one ester bond in two ester bonds of DOP is broken to generate benzoic acid (2-ethylhexyl) ester and 2-ethyl hexene, and the 2-ethyl hexene is hydrogenated to generate 3-methylheptane. The existence of the benzoic acid monoester can reduce the performance of preparing the cyclohexane plasticizer, and the alcohols and alkanes with low boiling points can cause the cyclohexane plasticizer to generate pungent odor, reduce the flash point of the cyclohexane plasticizer and finally reduce the comprehensive performance of the cyclohexane plasticizer, so that the research on the separation and purification of products of preparing the cyclohexane plasticizer by the liquid-phase hydrogenation of the o-benzene plasticizer is developed, and the industrialization is realized.
Disclosure of Invention
The invention aims to provide a production process for preparing cyclohexane plasticizer by performing liquid phase hydrogenation on o-benzene plasticizer capable of purifying cyclohexane plasticizer, which adopts the following technical scheme:
the production process of cyclohexane plasticizer by liquid phase hydrogenation of o-benzene plasticizer includes the following steps:
1) introducing heated inert gas to the bottom of the reduced pressure distillation tower in a pulse pneumatic transmission mode;
2) and the plasticizer product enters the bottom of the reduced pressure distillation tower after being preheated, and the inlet of the plasticizer product on the reduced pressure distillation tower is higher than the inlet of the inert gas, so that the plasticizer product is mixed and heated with the rising inert gas flow in the downward flowing process, and the target product and the by-product are separated.
The invention also aims to provide a system special for the production process of the cyclohexane plasticizer by the liquid-phase hydrogenation of the o-benzene plasticizer, and the technical scheme is as follows:
the production system for preparing the cyclohexane plasticizer by liquid-phase hydrogenation of the o-benzene plasticizer comprises a primary reduced pressure distillation tower and a secondary reduced pressure distillation tower which are connected in series through a separator, wherein the separator comprises a sleeve communicated between the tower bottom of the primary reduced pressure distillation tower and the tower top of the secondary reduced pressure distillation tower, a central pipe with a closed upper end and an open lower end is connected in the sleeve through a spoke-shaped support frame, the top of the central pipe extends out of the upper end of the sleeve and extends into the tower bottom of the primary reduced pressure distillation tower, an air release port is arranged on the pipe wall of the extending part, an inner baffle fixed on the pipe wall of the central pipe and an outer baffle fixed on the pipe wall of the sleeve are connected in an annular space between the central pipe and the sleeve, the inner baffle and the outer baffle are both inclined downwards and suspended, the inner baffle; the tower bottom of the first-stage reduced pressure distillation tower is provided with a plasticizer product inlet below the gas release port, the tower bottom of the second-stage reduced pressure distillation tower is provided with an inert gas inlet, the inert gas inlet is connected with an inert gas heater, and the inlet of the inert gas heater is connected with a gas source device controlled by a pulse generator.
Preferably, the vent holes are inclined holes which are inclined downwards from the tube cavity of the central tube, and the vent holes are positioned between two adjacent inner baffles and close to the upper baffle.
Preferably, the relief opening is an oblique hole sloping downward from the lumen of the central tube.
Preferably, the upper end of the central tube is conically shaped with the edge of the tap extending from the circumference of the central tube.
Preferably, the central tip of the tap cone is spherical crown shaped.
Preferably, the lower end of the central tube projects from the lower end of the sleeve and is provided with a flared air-receiving opening.
The invention has the beneficial effects that:
the process and the system of the invention adopt a pulse mode to send heated inert gas to the reduced pressure distillation tower, and utilize the characteristic that the time of the inert gas is large and small to better simulate fluidization mixing heating at the bottom of the reduced pressure distillation tower, thereby realizing better mixing heating and separation and purification effects on the plasticizer product, and having better separation and purification effects.
Drawings
FIG. 1 is a schematic view of a production system of the present invention;
fig. 2 is a schematic view of the separator of fig. 1.
Detailed Description
Referring to fig. 1, a schematic diagram of a production system for producing cyclohexane plasticizer by liquid phase hydrogenation of o-benzene plasticizer according to the present invention is shown, and the specific structure is as follows:
the device comprises a feeding preheater 1, a reduced pressure distillation tower 2, an extraction separation tower 3, a solvent regeneration tower 4, a light component tank 5, a heavy component tank 6, a first condenser 7, a second condenser 8, a first vacuum pump 9 and a second vacuum pump 10. The feeding preheater 1 is provided with a first feeding hole A, a first discharging hole B communicated with the first feeding hole A, a second feeding hole C and a second discharging hole D communicated with the second feeding hole C; the first condenser 7 and the second condenser 8 are respectively provided with a water inlet E, a water outlet F communicated with the water inlet E, a feed inlet G and a discharge outlet H communicated with the feed inlet G; an inert gas inlet K is formed in the bottom of the reduced pressure distillation tower 2, a heat conduction oil pipe 21 is arranged in an inner cavity of the bottom of the reduced pressure distillation tower 2 above the inert gas inlet K, and an oil inlet M and an oil outlet N of the heat conduction oil pipe 21 are both positioned outside the reduced pressure distillation tower 2; the reboiler 41 is connected to the bottom of the solvent regeneration column 4. The first discharge hole B of the feeding preheater 1 is connected to the middle part of the reduced pressure distillation tower 2, the tower bottom of the reduced pressure distillation tower 2 is connected with a distillation tower pump 22, the distillation tower pump 22 is connected to the second feed hole C of the feeding preheater 1, and the second discharge hole D of the feeding preheater 1 is divided into two branches which are respectively connected to the product tank 11 and the tower top of the reduced pressure distillation tower 2. The top of the reduced pressure distillation tower 2 is connected to the lower part of the extraction separation tower 3, the top of the extraction separation tower 3 is connected to the feed inlet G of the first condenser 7, the discharge outlet H of the first condenser 7 is connected to the light component tank 5, and the first condenser 7 and the light component tank 5 are connected to the first vacuum pump 9. The tower bottom of the extraction separation tower 3 is divided into two branches which are respectively connected to the tower top of the reduced pressure distillation tower 2 and the tower top of the solvent regeneration tower 4, the tower bottom of the solvent regeneration tower 4 is connected with a regeneration tower pump 42, the regeneration tower pump 42 is connected to the tower top of the extraction separation tower 3, the tower top of the solvent regeneration tower 4 is connected to a feed inlet G of the second condenser 8, a discharge hole H of the second condenser 8 is connected to the heavy component tank 6, and the second condenser 8 and the heavy component tank 6 are simultaneously connected to the second vacuum pump 10. The first vacuum pump 9 and the second vacuum pump 10 are both connected to the extraterrestrial region.
The vacuum distillation tower 2 includes a first vacuum distillation tower 25 and a first vacuum distillation tower 23 connected in series via a separator 24. Referring to fig. 2, the separator 24 includes a sleeve 241 communicated between the bottom of the first-stage vacuum distillation tower 25 and the top of the first-stage vacuum distillation tower 23, a central tube 242 with a closed upper end and an open lower end is connected to the sleeve 241 through a spoke-shaped support frame, the top of the central tube 242 extends from the upper end of the sleeve 241 and into the bottom of the first-stage vacuum distillation tower 25, and the wall of the extending part is provided with an air release opening 243, an inner baffle 244 fixed on the wall of the central tube 242 and an outer baffle 245 fixed on the wall of the sleeve 241 are connected to the annular space between the central tube 242 and the sleeve 241, the inner baffle 244 and the outer baffle 245 are both suspended in a downward inclined manner, the inner baffle 244 and the outer baffle 245 are alternately distributed from top to bottom, and a vent hole 246 located; the tower bottom of the first-stage reduced pressure distillation tower 25 is provided with a plasticizer product inlet positioned below the air release port 243, the tower bottom of the first-stage reduced pressure distillation tower 23 is provided with an inert gas inlet, the inert gas inlet is connected with an inert gas heater 27, and the inlet of the inert gas heater 27 is connected with a gas source device 26 controlled by a pulse generator.
The air release hole 243 and the air vent hole 246 are inclined holes inclined downward from the lumen of the central tube 242, and the air vent hole 246 is located between two adjacent inner baffle plates 244 at a position near the upper one. The upper end of the central tube 242 is conically tapered with the edge of the taper extending from the periphery of the central tube 242. The central tip of the shunting cone is in a spherical crown shape. The lower end of the center tube 242 protrudes from the lower end of the sleeve 241 and is provided with a flared air-receiving opening.
The production process comprises the following steps:
(1) introducing heated N2 gas to the bottom of the reduced pressure distillation tower 2 in a pulse pneumatic conveying mode, introducing heat conduction oil into a heat conduction oil pipe 21, adding an extraction solvent N, N-Dimethylacetamide (DMAC) into the extraction separation tower 3, starting a reboiler 41 of a solvent regeneration tower 4, and introducing circulating water into a first condenser 7 and a second condenser 8 respectively; the operating temperature of the reduced pressure distillation tower 2 is controlled to be 260 ℃, the operating temperature of the extraction separation tower 3 is controlled to be 140 ℃, and the operating temperature of the solvent regeneration tower 4 is controlled to be 200 ℃; the interior of a reduced pressure distillation tower 2, an extraction separation tower 3, a solvent regeneration tower 4, a light component tank 5, a heavy component tank 6, a first condenser 7 and a second condenser 8 are all kept in a negative pressure state, and the pressure is-0.08 MPa;
(2) sampling and analyzing a hydrogenation product, detecting the conversion rate of a raw material DOP and the selectivity and yield of a product DEHCH by using gas chromatography, confirming that the conversion rate of the DOP reaches 100%, carrying out settling separation, allowing the hydrogenation product without the catalyst to enter a feeding preheater 1 from a first feeding hole A of the feeding preheater 1, preheating, then allowing the hydrogenation product to enter a reduced pressure distillation tower 2 from a first discharging hole B, carrying out mass transfer heating on a downward flowing and rising N2 gas flow, and separating a target product from a byproduct;
(3) the target product enters the bottom of the reduced pressure distillation tower 2, is extracted from the bottom of the tower and is sent to a second feed inlet C through a distillation tower pump 22 to enter a feed preheater 1 to exchange heat with the hydrogenation product, the target product after heat exchange is detected to be qualified and is sent to a product tank 11, and if the target product is not qualified, the target product is sent to the top of the reduced pressure distillation tower 2 to enter the reduced pressure distillation tower 2 again for distillation treatment; the by-product enters the extraction separation tower 3 along with the tower top N2 gas of the reduced pressure distillation tower 2, and after being extracted and separated by an extraction solvent N, N-Dimethylacetamide (DMAC) in the extraction separation tower 3, light components and heavy components in the by-product are separated;
(4) the light components enter a first condenser 7 along with part of N2 gas from the top of the extraction separation tower 3, the light components enter a light component tank 5 after being condensed by circulating water introduced into the first condenser 7, and N2 gas is pumped out by a first vacuum pump 9 as non-condensable gas and is sent to an out-of-range area; heavy components and N, N-Dimethylacetamide (DMAC) enter a solvent regeneration tower 4 from the bottom of an extraction separation tower 3, the heavy components and the N, N-Dimethylacetamide (DMAC) are separated and then enter a second condenser 8 along with part of N2 gas, the heavy components and the N, N-Dimethylacetamide (DMAC) are condensed and liquefied by circulating water introduced into the second condenser 8 and then enter a heavy component tank 6, and N2 gas serving as non-condensable gas is pumped out by a second vacuum pump 10 and sent to an out-of-range area; the N, N-dimethylacetamide DMAC is regenerated and returned to the top of the extraction separation tower 3 through a regeneration tower pump 42, the N, N-dimethylacetamide DMAC is returned to the top of the reduced pressure distillation tower 2 from the bottom of the extraction separation tower 3 for recycling, and the N, N-dimethylacetamide DMAC and the byproduct enter the extraction separation tower 3 together with the N2 gas at the top of the reduced pressure distillation tower 2 after being treated by the reduced pressure distillation tower 2;
wherein, the light component refers to low boiling point alcohol and alkane, and the heavy component refers to cyclohexane monoacid ester.
The above description is only about the preferred embodiment of the present invention, but it should not be understood as limiting the claims, and the present invention may be modified in other structures, not limited to the above structures. In general, all changes which come within the scope of the invention are intended to be embraced therein.
Claims (5)
1. The production system for preparing the cyclohexane plasticizer by liquid-phase hydrogenation of the o-benzene plasticizer is characterized by comprising a primary reduced pressure distillation tower and a secondary reduced pressure distillation tower which are connected in series through a separator, wherein the separator comprises a sleeve communicated between the tower bottom of the primary reduced pressure distillation tower and the tower top of the secondary reduced pressure distillation tower, a central pipe with the upper end closed and the lower end opened is connected in the sleeve through a spoke-shaped support frame, the top of the central pipe extends out of the upper end of the sleeve and extends into the tower bottom of the primary reduced pressure distillation tower, a gas release port is arranged on the pipe wall of the extending part, an inner baffle fixed on the pipe wall of the central pipe and an outer baffle fixed on the wall of the sleeve are connected in an annular space between the central pipe and, the inner baffle and the outer baffle are alternately distributed from top to bottom, and a vent hole positioned on the pipe wall of the central pipe is arranged below the root part of the inner baffle; the tower bottom of the first-stage reduced pressure distillation tower is provided with a plasticizer product inlet positioned below the gas release port, the tower bottom of the second-stage reduced pressure distillation tower is provided with an inert gas inlet, the inert gas inlet is connected with an inert gas heater, and the inlet of the inert gas heater is connected with a gas source device controlled by a pulse generator; the lower end of the central tube extends out of the lower end of the sleeve and is provided with a horn-shaped air collecting opening.
2. The production system for producing cyclohexane plasticizer by liquid phase hydrogenation of o-benzene plasticizer according to claim 1, wherein the vent hole is an inclined hole inclined downward from the tube cavity of the central tube, and the vent hole is located between two adjacent internal baffles at a position close to the upper one.
3. The production system for producing cyclohexane plasticizer according to claim 1, wherein the gas release port is an inclined hole inclined downward from the tube cavity of the central tube.
4. The production system for producing cyclohexane plasticizer by liquid phase hydrogenation of phthalic acid plasticizer according to claims 1 to 3, wherein the central tube has a conical upper end diverging cone, and the edge of the diverging cone extends from the periphery of the central tube.
5. The system for producing cyclohexane-based plasticizer by liquid phase hydrogenation of o-benzene-based plasticizer according to claim 4, wherein the central tip of the diverging cone has a spherical crown shape.
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| CN107759471B (en) * | 2017-12-05 | 2023-08-11 | 郑州大学 | Separation and purification device and process for preparing cyclohexane plasticizer product by liquid phase hydrogenation of o-benzene plasticizer |
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