CN116059674B - A combined system for the hydroformylation reaction and separation of high-carbon chain olefins - Google Patents

A combined system for the hydroformylation reaction and separation of high-carbon chain olefins

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Publication number
CN116059674B
CN116059674B CN202310099862.3A CN202310099862A CN116059674B CN 116059674 B CN116059674 B CN 116059674B CN 202310099862 A CN202310099862 A CN 202310099862A CN 116059674 B CN116059674 B CN 116059674B
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vacuum
tower
outlet
reactor
inlet
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CN116059674A (en
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朱博源
王晓明
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Meryer Technologies Co Ltd
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Meryer Technologies Co Ltd
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    • 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
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • 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
    • B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
    • 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
    • B01D3/02—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in boilers or stills
    • 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
    • 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
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322—Reboiler specifications
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B01J8/0085—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction promoting uninterrupted fluid flow, e.g. by filtering out particles in front of the catalyst layer
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/082—Controlling processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/085—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • B01J8/224—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement
    • B01J8/228—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
    • C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/78—Separation; Purification; Stabilisation; Use of additives
    • C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
    • C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

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  • Crystallography & Structural Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

本发明公开了一种高碳链烯烃氢甲酰化反应和分离的组合系统，包括一级反应釜、二级反应釜、三级反应釜、高压废气冷却器、高压分离罐、真空泵、减压脱重塔、减压脱重塔顶冷却器、减压脱重塔顶回流罐、减压脱重塔底泵、减压脱重塔顶回流泵、减压脱重塔底再沸器、减压脱轻塔进料换热器、减压脱轻塔、减压脱轻塔顶冷却器、减压脱轻塔顶回流罐、减压脱轻塔底泵、减压脱轻塔顶回流泵、减压脱轻塔底再沸器、合成气进料缓冲罐、合成气净化器、烯烃净化器、烯烃/催化剂混合器。本发明的反应转化率较高、反应选择性较好，目标产物纯度高，催化剂回收率大幅提高，降低运行成本。

This invention discloses a combined system for the hydroformylation reaction and separation of high-carbon chain olefins, comprising a primary reactor, a secondary reactor, a tertiary reactor, a high-pressure waste gas cooler, a high-pressure separation tank, a vacuum pump, a vacuum deweighting tower, a vacuum deweighting tower top cooler, a vacuum deweighting tower top reflux tank, a vacuum deweighting tower bottom pump, a vacuum deweighting tower top reflux pump, a vacuum deweighting tower bottom reboiler, a vacuum delighting tower feed heat exchanger, a vacuum delighting tower, a vacuum delighting tower top cooler, a vacuum delighting tower top reflux tank, a vacuum delighting tower bottom pump, a vacuum delighting tower top reflux pump, a vacuum delighting tower bottom reboiler, a syngas feed buffer tank, a syngas purifier, an olefin purifier, and an olefin/catalyst mixer. This invention features high reaction conversion rate, good reaction selectivity, high target product purity, significantly improved catalyst recovery rate, and reduced operating costs.

Description

Combined system for hydroformylation reaction and separation of high carbon chain olefins
Technical Field
The invention relates to a high carbon chain olefin hydroformylation reaction and separation combined system, and belongs to the technical field of chemical reaction system equipment.
Background
The hydroformylation reaction of olefins, also known as OXO (OXO) reaction, refers to the reaction of olefins with carbon monoxide and hydrogen under the action of a transition metal complex catalyst to produce normal, isomeric aldehydes having one more carbon atom than the starting olefins.
R-CH=CH2+ H2+ CO R-CH2-CH2-CHO or R-CH(CHO)-CH3
The reaction is also called hydroformylation, since a hydrogen atom and a formyl group are added to the carbon atoms at both ends of the double bond of the unsaturated compound.
The hydroformylation reaction has achieved remarkable results over many years, and the oxo industry has become the most important organic synthesis industry worldwide. The olefin hydroformylation reaction is a typical homogeneous complex catalytic reaction, has the advantages of high catalyst activity and good selectivity, is often used for producing aldehydes and alcohols widely applied in the field of refinement industry in industry, can be used for synthesizing surfactants, fabric additives and plasticizers, can be used for producing various medical intermediates in the pharmaceutical industry, and can be further processed into spices for the food industry. The hydroformylation reaction of olefin belongs to an atomic economic reaction, atoms in the synthesis gas all enter olefin, no waste and substances toxic and harmful to the environment are generated, the hydroformylation reaction is a recognized green chemical process, meets the requirement of sustainable development, and is now the field of chemical industry and key research which are developed at home and abroad, but the problems of product separation and catalyst recycling still exist.
Cobalt-based catalysts are the earliest catalysts for the industrial production of olefin hydroformylation, but the reaction requires high pressure to maintain the stability of the active substances of the catalysts, high temperature to increase the reaction rate, and high temperature and high pressure operating conditions increase the difficulty and risk of industrial production. Later, rhodium was found to be a metal having a hydroformylation reaction activity more than cobalt, and the rhodium catalyst was found to have a low operating pressure and a good safety as compared with the cobalt catalyst. Although the new rhodium phosphine catalyst reduces the production condition of olefin hydroformylation, has the advantages of mild reaction condition, high positive-to-negative ratio of products and good heat transfer effect, and shows excellent economic effect, the catalyst is difficult to recover because rhodium is noble metal, so that the popularization and application of the catalyst are limited.
In order to solve the problem of difficult separation of the oil-soluble rhodium phosphine complex catalyst and the product, a water/organic two-phase catalytic system is developed, wherein the catalyst is dissolved in water, so that the contact of the catalyst with toxic substances in an organic phase is avoided, and the service life of the catalyst is prolonged. The product is dissolved in an organic phase, and after the reaction is finished, the catalyst and the product can be separated through simple standing layering, so that rhodium loss in the distillation process of the oil-soluble catalyst is reduced. However, the water solubility of long-chain olefins greatly limits the mass transfer rate of the oil-water reaction interface, resulting in extremely low reaction rates and conversions of about 20%. Mainly because in the water/organic two-phase catalytic system, the oxo reaction rate is mainly limited by the solubility of olefin in water, the water-soluble rhodium phosphine complex catalytic system is only applicable to low-carbon olefin. Limited by the recovery of the catalyst, the development of the hydroformylation process of the long carbon chain olefin is slower, and the industrialization degree of the domestic technology is lower.
Disclosure of Invention
The invention aims to solve the technical problems of providing a high carbon chain olefin hydroformylation reaction and separation combined system which is used for producing high carbon aldehyde by the hydroformylation reaction of high carbon olefin, can efficiently recycle the catalyst in the reaction process while improving the conversion rate, the selectivity and the purity of the high carbon aldehyde, reduces the loss of a noble metal rhodium catalyst, reduces the running cost and increases the economic benefit.
The invention solves the technical problems by the following technical proposal:
a combined system for hydroformylation and separation of high carbon olefins comprising:
The device comprises a first-stage reaction kettle, a second-stage reaction kettle and a third-stage reaction kettle, wherein the top of each reaction kettle is provided with an air outlet, one side of the upper part is provided with a feed inlet, one side of the lower part is provided with an air inlet, and the bottom is provided with a discharge outlet;
The outer sides of the primary reaction kettle, the secondary reaction kettle and the tertiary reaction kettle are respectively provided with a jacket, the bottom of each jacket is provided with a water inlet, and the upper part of each jacket is provided with a water return port;
The olefin/catalyst mixer is communicated with a feed inlet of the primary reaction kettle through an olefin heater, a discharge outlet of the primary reaction kettle is communicated with a feed inlet of the secondary reaction kettle, and a discharge outlet of the secondary reaction kettle is communicated with a feed inlet of the tertiary reaction kettle;
The synthesis gas buffer tank is characterized in that one side of the synthesis gas buffer tank is provided with an air inlet communicated with synthesis gas, the bottom of the synthesis gas buffer tank is provided with a sewage outlet, the top of the synthesis gas buffer tank is provided with an air outlet, and the air outlet is respectively communicated with the air inlets of the primary reaction kettle, the secondary reaction kettle and the tertiary reaction kettle through a synthesis gas heater;
The high-pressure separation tank is provided with an air inlet at one side, an air outlet at the top and a water return port at the bottom, the air outlet of the three-stage reaction kettle is communicated with the air inlet of the high-pressure separation tank through a high-pressure waste gas cooler, the air outlet of the high-pressure separation tank is communicated with the air inlet of the synthetic gas buffer tank, and the water return port of the high-pressure separation tank is communicated with the three-stage reaction kettle;
The device comprises a pressure reducing and weight removing tower, wherein an air outlet is formed in the top of the pressure reducing and weight removing tower, a feed inlet is formed in one side of the middle of the pressure reducing and weight removing tower, a discharge outlet is formed in the bottom of the pressure reducing and weight removing tower, a return port is formed in one side of the upper of the pressure reducing and weight removing tower, the feed inlet of the pressure reducing and weight removing tower is communicated with the discharge outlet of a three-stage reaction kettle, and the discharge outlet of the pressure reducing and weight removing tower is communicated with an olefin/catalyst mixer through a pressure reducing and weight removing tower bottom pump;
The top of the pressure-reducing heavy-removal tower top reflux tank is provided with a feed inlet and an air outlet, the bottom of the pressure-reducing heavy-removal tower top reflux tank is provided with a liquid outlet, the air outlet of the pressure-reducing heavy-removal tower is communicated with the feed inlet of the pressure-reducing heavy-removal tower top reflux tank through a pressure-reducing heavy-removal tower top cooler, the air outlet of the pressure-reducing heavy-removal tower top reflux tank is communicated with the inlet end of a vacuum pump, and the liquid outlet of the pressure-reducing heavy-removal tower top reflux tank is communicated with the reflux inlet of the pressure-reducing heavy-removal tower through a pressure-reducing heavy-removal tower top reflux pump;
The top of the decompression and light component removing tower is provided with an air outlet, one side of the middle part is provided with a feed inlet, the bottom is provided with a discharge outlet, one side of the upper part is provided with a reflux inlet, the feed inlet of the decompression and light component removing tower is communicated with the outlet end of a reflux pump at the top of the decompression and heavy component removing tower, and the discharge outlet of the decompression and light component removing tower is discharged through a pump at the bottom of the decompression and light component removing tower to obtain a high-carbon aldehyde product; the bottom of the decompression light component removing tower is connected with a heat source through a decompression light component removing tower bottom reboiler;
The top of the pressure-reducing light-removing tower top reflux tank is provided with a feed inlet and an air outlet, the bottom of the pressure-reducing light-removing tower top reflux tank is provided with a liquid outlet, the feed inlet of the pressure-reducing light-removing tower top reflux tank is communicated with the air outlet of the pressure-reducing light-removing tower through a pressure-reducing light-removing tower top cooler, the air outlet of the pressure-reducing light-removing tower top reflux tank is communicated with the inlet end of a vacuum pump, and the liquid outlet of the pressure-reducing light-removing tower top reflux tank is respectively communicated with a reflux port of the pressure-reducing light-removing tower and a high-carbon olefin feed line through the pressure-reducing light-removing tower top reflux pump.
Preferably, cold sources of the decompression and heavy removal tower top cooler and the decompression and light removal tower top cooler all adopt chilled water.
Preferably, an olefin purifier is provided before the inlet end of the olefin/catalyst mixer.
Preferably, the gas outlet of the synthesis gas buffer tank is sequentially provided with a synthesis gas supercharger and a synthesis gas purifier.
Preferably, the pipeline between the pressure-reducing heavy-removal tower top reflux pump and the pressure-reducing light-removal tower feed inlet and the discharge pipeline of the pressure-reducing light-removal tower bottom pump exchange heat through the pressure-reducing light-removal tower feed heat exchanger.
Compared with the prior art, the invention has the beneficial effects that:
the single pass conversion rate of high carbon chain olefin is more than or equal to 80 percent, the target high carbon aldehyde selectivity is more than or equal to 95 percent, and the high carbon aldehyde purity is more than or equal to 99 percent;
The reaction condition is mild, the reaction temperature is less than or equal to 90 ℃, and the reaction pressure is less than or equal to 2.0MPa;
The pressure reduction rectification mode is adopted, the temperature of the bottom of the rectification tower is reduced, the catalyst temperature is kept within the activity maximum interval, the catalyst deactivation rate is reduced, the catalyst recovery rate is more than or equal to 99% at the beginning of operation, and the activity of the recovered catalyst is more than or equal to 95%;
Adopting an excessive synthesis gas recovery technology, wherein the recovery rate of the synthesis gas is more than or equal to 99.9%;
The reaction condition is mild, the recovery rate of catalyst and synthesis gas is high, the running cost of the device is reduced by more than 30 percent.
Drawings
FIG. 1 is a schematic diagram of a combined system for hydroformylation and separation of high carbon chain olefins provided by the invention.
Detailed Description
In order to make the invention more comprehensible, preferred embodiments accompanied with figures are described in detail below.
Examples
As shown in FIG. 1, the invention provides a combined system for hydroformylation and separation of high carbon chain olefins, which comprises:
The gas outlet of the first-stage reaction kettle 1 is communicated with the gas inlet of the second-stage reaction kettle 2 through a first-stage reaction kettle top gas phase line 45, and the gas outlet of the second-stage reaction kettle 2 is communicated with the gas inlet of the third-stage reaction kettle 3 through a second-stage reaction kettle top gas phase line 46;
The circulating water inlet bus 63 is respectively communicated with the water inlets of the three jackets through a circulating water inlet line I64, a circulating water inlet line II 65 and a circulating water inlet line III 66, and the circulating water return bus 70 is respectively communicated with the water return ports of the three jackets through a circulating water return line I67, a circulating water return line II 68 and a circulating water return line III 69;
The high-carbon olefin feeding line 77 is communicated with a feeding port of the first-stage reaction kettle 1 through an olefin purifier 22, a mixed gas feeding line 78, the olefin/catalyst mixer 23, an olefin heater feeding line 79, an olefin heater 24 and an olefin heater outlet line 80 in sequence, a discharging port of the first-stage reaction kettle 1 is communicated with a feeding port of the second-stage reaction kettle 2 through a second-stage reaction kettle feeding line 27, a discharging port of the second-stage reaction kettle 2 is communicated with a feeding port of the third-stage reaction kettle 3 through a third-stage reaction kettle feeding line 28, and the olefin/catalyst mixer 23 is also communicated with a catalyst supplementing line 54 for supplementing catalyst;
The synthesis gas buffer tank 20 is provided with an air inlet at one side of the synthesis gas buffer tank 20, a drain outlet at the bottom and an air outlet at the top, wherein the synthesis gas is communicated with the air inlet through a synthesis gas buffer tank inlet line 39, the air outlet is sequentially communicated with a synthesis gas buffer tank outlet line 40, a synthesis gas booster 26, a synthesis gas booster outlet line 76, a synthesis gas purifier 21, a purified synthesis gas bus 41, a synthesis gas heater 25 and a synthesis gas heater outlet line 81, and the synthesis gas heater outlet line 81 is respectively communicated with the air inlet of the first-stage reaction kettle 1, the air inlet of the second-stage reaction kettle 2 and the air inlet of the third-stage reaction kettle 3 through a purified synthesis gas line I42, a purified synthesis gas line II and a purified synthesis gas line III 44;
The high-pressure separation tank 5 is characterized in that an air inlet is formed in one side of the high-pressure separation tank 5, an air outlet is formed in the top of the high-pressure separation tank 5, a water return port is formed in the bottom of the high-pressure separation tank, the air outlet of the three-stage reaction kettle 3 is sequentially communicated with the air inlet of the high-pressure separation tank 5 through a three-stage reaction kettle top gas phase line 47, a high-pressure waste gas cooler 4 and a high-pressure waste gas cooler outlet line 48, the air outlet of the high-pressure separation tank 5 is sequentially communicated with the synthetic gas buffer tank inlet line 39 through a high-pressure separation tank gas phase line 52 and a vacuum pump outlet line 53, and the water return port of the high-pressure separation tank 5 is communicated with the upper part of the three-stage reaction kettle 3 through a high-pressure separation tank water return line 82;
The pressure-reducing weight-reducing tower 7, wherein an air outlet is formed in the top of the pressure-reducing weight-reducing tower 7, a feed inlet is formed in one side of the middle of the pressure-reducing weight-reducing tower 7, a discharge outlet is formed in the bottom of the pressure-reducing weight-reducing tower 7, a return port is formed in one side of the upper of the pressure-reducing weight-reducing tower 7, the feed inlet of the pressure-reducing weight-reducing tower 7 is communicated with the discharge outlet of the three-stage reaction kettle 3 through a pressure-reducing weight-reducing tower feed line 29, the discharge outlet of the pressure-reducing weight-reducing tower 7 is communicated with the olefin/catalyst mixer 23 through a pressure-reducing weight-reducing tower outlet line 56, a pressure-reducing weight-reducing tower pump 10 and a pressure-reducing weight-reducing tower pump outlet line 55 in turn, the bottom of the pressure-reducing weight-reducing tower 7 is connected with a heat source through a pressure-reducing weight-reducing tower reboiler 12, the pressure-reducing weight-reducing tower reboiler 12 is provided with a pressure-reducing weight-reducing tower reboiler heat source feed line 72, and a pressure source outlet line 73;
The top of the pressure-reducing heavy-removal tower top reflux tank 9 is provided with a feed inlet and an air outlet, the bottom of the pressure-reducing heavy-removal tower top reflux tank 9 is provided with a liquid outlet, the air outlet of the pressure-reducing heavy-removal tower 7 is communicated with the air inlet of the pressure-reducing heavy-removal tower top reflux tank 9 sequentially through a pressure-reducing heavy-removal tower gas phase line 30, a pressure-reducing heavy-removal tower top cooler 8 and a pressure-reducing heavy-removal tower top cooler outlet line 31, the air outlet of the pressure-reducing heavy-removal tower top reflux tank 9 is communicated with a gas phase sink bus 51 through a pressure-reducing heavy-removal tower top gas phase line 49, the liquid outlet of the pressure-reducing heavy-removal tower top reflux tank 9 is communicated with a pressure-reducing heavy-removal tower reflux line 33 and a pressure-reducing light-removal tower feed line 34 sequentially through a pressure-reducing heavy-removal tower reflux pump 11 respectively, and the pressure-reducing heavy-removal tower reflux line 33 is communicated with a reflux port of the pressure-reducing heavy-removal tower 7;
The vacuum light component removing tower 14 comprises a top of the vacuum light component removing tower 14, a bottom of the vacuum light component removing tower 14, a vacuum light component removing tower reboiler, a vacuum light component removing tower heat source outlet line 75, a vacuum light component removing tower reboiler heat source outlet line 36, a vacuum light component removing tower bottom pump 17, a vacuum light component removing tower outlet line 37, a vacuum light component removing tower feed line I and a high-carbon aldehyde product line 38, wherein an air outlet is arranged at the top of the vacuum light component removing tower 14, a feed inlet is arranged at one side of the middle, a discharge outlet is arranged at the bottom of the vacuum light component removing tower 14, a return inlet is arranged at one side of the upper part, the feed inlet of the vacuum light component removing tower 14 is communicated with the vacuum light component removing tower feed heat exchanger 13 through a vacuum light component removing tower feed line II 35, and the discharge outlet of the vacuum light component removing tower 14 is sequentially discharged through the vacuum light component removing tower bottom line 36, the vacuum light component removing tower pump 17, the vacuum light component removing tower feed line I and the high-carbon aldehyde product line 38;
The top of the vacuum light-removal tower top reflux tank 16 is provided with a feed inlet and an air outlet, the bottom of the vacuum light-removal tower top reflux tank 16 is provided with a liquid outlet, the feed inlet of the vacuum light-removal tower top reflux tank 16 is sequentially communicated with the air outlet of the vacuum light-removal tower 14 through a vacuum light-removal tower top cooler discharge line 58, a vacuum light-removal tower top cooler 15 and a vacuum light-removal tower top gas phase line 57, the air outlet of the vacuum light-removal tower top reflux tank 16 is communicated with a gas phase sink line 51 through a vacuum light-removal tower top reflux tank gas phase line 50, the gas phase sink line 51 is communicated with a vacuum pump 6, the liquid outlet of the vacuum light-removal tower top reflux tank 16 is sequentially communicated with a vacuum light-removal tower top reflux line 61 and a high-carbon olefin recovery line 62 through a vacuum light-removal tower top reflux pump outlet line 60, and the vacuum light-removal tower top reflux line 61 is communicated with the reflux inlet of the vacuum light-removal tower 14, and the high-carbon olefin recovery line 62 is communicated with the high-carbon olefin feed line 77. The pipeline of the first pressure reduction light ends removing tower feeding line 34/the second pressure reduction light ends removing tower feeding line 35 and the pipeline of the pressure reduction light ends removing tower bottom outlet line 37/the high-carbon aldehyde product line 38 exchange heat through the pressure reduction light ends removing tower feeding heat exchanger 13. Chilled water is adopted as cold sources of the decompression and weight removal tower top cooler 8 and the decompression and weight removal tower top cooler 15.
The invention adopts a kettle type reactor, the mixed solution of high-carbon olefin and catalyst enters from the upper part of the side surface of the reactor, synthesis gas enters from the lower part of the side surface of the reactor, tiny bubbles are formed after passing through a gas distributor, hydroformylation reaction is carried out by countercurrent contact between the synthesis gas and the high-carbon olefin and the catalyst in the reactor, the reacted liquid phase product is self-pressed to the next stage reactor through a kettle bottom outlet, and the reacted gas phase is led to the next stage reactor through a kettle top gas phase outlet to be converged with the synthesis gas and then enters into the reaction kettle. The reaction adopts a catalyst with noble metal rhodium as a main body, the reaction activity is greatly improved, the reaction pressure is controlled within 2.0MPa, three-stage series reactors are arranged in the reaction, the requirement of residence time is ensured, the conversion rate of the reaction is improved to more than 80 percent under the action of the catalyst, and the selectivity of the reaction is improved to 95 percent;
Because the hydroformylation reaction catalyst is noble metal, the activity of the catalyst is easy to be deactivated by being polluted by other impurities, so that the reaction conversion rate is reduced, and the selectivity is reduced. The invention adopts the high-efficiency olefin purifier, the purifier adopts a skid-mounted type to treat the impurities (sulfur, oxygen, metal and the like) carried by the high-carbon olefin, so that the impurity content of the high-carbon olefin can be reduced to below 0.05ppm (mol), the cleanliness of the high-carbon olefin entering a reaction system is ensured, and the maximum performance of the catalyst is further ensured.
The method adopts a form of pressurizing and recycling the synthesis gas by a vacuum pump, so that the loss of the synthesis gas with excessive reaction is avoided. The gas phase at the top of the pressure-reducing and weight-removing tower top reflux tank and the gas phase at the top of the pressure-reducing and weight-removing tower top reflux tank are converged by a vacuum pump and then are sent back to the synthetic gas buffer tank again, so that the loss of the synthetic gas after reaction is ensured to be less than 0.1%, and meanwhile, the vacuum pump also plays a role in adjusting the vacuum degree of the rectifying tower while controlling the pressure.
Because the hydroformylation reaction catalyst is noble metal, the activity of the catalyst is easy to be deactivated by being polluted by other impurities, so that the reaction conversion rate is reduced, and the selectivity is reduced. The invention adopts the high-efficiency synthetic gas purifier, the purifier adopts a skid-mounted type to treat the impurities (sulfur, oxygen, metal and the like) carried by the synthetic gas, the impurity content of the synthetic gas can be reduced to below 0.05ppm (mol), the cleanliness of the synthetic gas entering a reaction system is ensured, and the maximum performance of the catalyst is further ensured.
In general, as the boiling point of high-carbon hydrocarbon is higher, when the high-carbon hydrocarbon and the catalyst are separated in a rectification mode, the temperature at the bottom of the rectification tower is ultrahigh to deactivate the noble metal catalyst, so that the catalyst is lost, and after the pressure reduction rectification mode is adopted, the pressure distribution of the whole rectification tower is reduced in a pressure reduction heavy removal rectification tower, the corresponding saturation temperature is reduced, the boiling point of the high-carbon hydrocarbon is reduced, the temperature at the bottom of the tower is also reduced along with the reduction of the high-carbon hydrocarbon, so that the catalyst temperature is always less than or equal to 95 ℃, the service life of the catalyst is effectively prolonged, the daily consumption is reduced, the operation cost is saved, and the pressure reduction light removal rectification tower effectively reduces the boiling point of a medium by utilizing pressure reduction, so that the high-efficiency separation of the high-carbon hydrocarbon and high-carbon aldehyde is realized, and the purity of the high-carbon aldehyde is more than or equal to 99%.

Claims (5)

1.一种高碳链烯烃氢甲酰化反应和分离的组合系统，其特征在于，包括：1. A combined system for the hydroformylation reaction and separation of high-carbon chain olefins, characterized in that it comprises: 一级反应釜（1）、二级反应釜（2）、三级反应釜（3）：每个反应釜的顶部设有出气口，上部的一侧设有进料口，下部的一侧设有进气口，底部设有出料口；一级反应釜（1）的出气口与二级反应釜（2）的进气口连通，二级反应釜（2）的出气口与三级反应釜（3）的进气口连通；Primary reactor (1), secondary reactor (2), tertiary reactor (3): Each reactor has an outlet at the top, a feed inlet on one side of the upper part, an air inlet on one side of the lower part, and a discharge outlet at the bottom; the outlet of the primary reactor (1) is connected to the air inlet of the secondary reactor (2), and the outlet of the secondary reactor (2) is connected to the air inlet of the tertiary reactor (3); 一级反应釜（1）、二级反应釜（2）、三级反应釜（3）外侧均设有夹套，每个夹套的底部设有进水口，上部设有回水口；The first-stage reactor (1), the second-stage reactor (2), and the third-stage reactor (3) are all equipped with jackets on the outside. Each jacket has a water inlet at the bottom and a water return outlet at the top. 用于将高碳烯烃与催化剂混合的烯烃/催化剂混合器（23）：烯烃/催化剂混合器（23）通过烯烃加热器（24）与一级反应釜（1）的进料口连通；一级反应釜（1）的出料口与二级反应釜（2）的进料口连通；二级反应釜（2）的出料口与三级反应釜（3）的进料口连通；Olefin/catalyst mixer (23) for mixing high carbon olefins with catalyst: The olefin/catalyst mixer (23) is connected to the feed port of the primary reactor (1) via an olefin heater (24); the discharge port of the primary reactor (1) is connected to the feed port of the secondary reactor (2); the discharge port of the secondary reactor (2) is connected to the feed port of the tertiary reactor (3); 合成气缓冲罐（20）：合成气缓冲罐（20）的一侧设有与合成气连通的进气口，合成气通过合成气缓冲罐进口线（39）与进气口连通；底部设有排污口，顶部设有出气口，该出气口通过合成气加热器（25）分别与一级反应釜（1）、二级反应釜（2）、三级反应釜（3）的进气口连通；Syngas buffer tank (20): One side of the syngas buffer tank (20) is provided with an air inlet that is connected to the syngas. The syngas is connected to the air inlet through the syngas buffer tank inlet line (39); the bottom is provided with a drain outlet and the top is provided with an outlet. The outlet is connected to the air inlets of the first-stage reactor (1), the second-stage reactor (2), and the third-stage reactor (3) through the syngas heater (25); 高压分离罐（5）：高压分离罐（5）的一侧设有进气口，顶部设有出气口，底部设有回水口，三级反应釜（3）的出气口通过高压废气冷却器（4）与高压分离罐（5）的进气口连通，高压分离罐（5）的出气口依次通过高压分离罐气相线（52）、真空泵出口线（53）与合成气缓冲罐进口线（39）连通，高压分离罐（5）的回水口与三级反应釜（3）连通；High pressure separator (5): The high pressure separator (5) has an air inlet on one side, an air outlet on the top, and a water return outlet at the bottom. The air outlet of the three-stage reactor (3) is connected to the air inlet of the high pressure separator (5) through the high pressure waste gas cooler (4). The air outlet of the high pressure separator (5) is connected to the inlet line of the synthesis gas buffer tank (39) in sequence through the high pressure separator gas phase line (52) and the vacuum pump outlet line (53). The water return outlet of the high pressure separator (5) is connected to the three-stage reactor (3). 减压脱重塔（7）：减压脱重塔（7）的顶部设有出气口，中部的一侧设有进料口，底部设有出料口，上部的一侧设有回流口，减压脱重塔（7）的进料口与三级反应釜（3）的出料口连通，减压脱重塔（7）的出料口通过减压脱重塔底泵（10）与烯烃/催化剂混合器（23）连通；所述减压脱重塔（7）的底部通过减压脱重塔底再沸器（12）连接热源；Vacuum-reduced deweighting tower (7): The vacuum-reduced deweighting tower (7) has an outlet at the top, a feed inlet on one side of the middle, a discharge outlet at the bottom, and a reflux outlet on one side of the upper part. The feed inlet of the vacuum-reduced deweighting tower (7) is connected to the discharge outlet of the three-stage reactor (3). The discharge outlet of the vacuum-reduced deweighting tower (7) is connected to the olefin/catalyst mixer (23) through the vacuum-reduced deweighting tower bottom pump (10). The bottom of the vacuum-reduced deweighting tower (7) is connected to a heat source through the vacuum-reduced deweighting tower bottom reboiler (12). 减压脱重塔顶回流罐（9）：减压脱重塔顶回流罐（9）顶部设有进料口、出气口，底部设有出液口，减压脱重塔（7）的出气口通过减压脱重塔顶冷却器（8）与减压脱重塔顶回流罐（9）的进气口连通，减压脱重塔顶回流罐（9）的出气口与真空泵（6）的进口端连通，减压脱重塔顶回流罐（9）的出液口通过减压脱重塔顶回流泵（11）与减压脱重塔（7）的回流口连通；Top reflux tank (9) of vacuum decompression tower: The top reflux tank (9) of vacuum decompression tower is provided with a feed inlet and an air outlet at the top and a liquid outlet at the bottom. The air outlet of vacuum decompression tower (7) is connected to the air inlet of vacuum decompression tower top reflux tank (9) through vacuum decompression tower top cooler (8). The air outlet of vacuum decompression tower top reflux tank (9) is connected to the inlet end of vacuum pump (6). The liquid outlet of vacuum decompression tower top reflux tank (9) is connected to the reflux port of vacuum decompression tower (7) through vacuum decompression tower top reflux pump (11). 减压脱轻塔（14）：减压脱轻塔（14）的顶部设有出气口，中部的一侧设有进料口，底部设有出料口，上部的一侧设有回流口，减压脱轻塔（14）的进料口与减压脱重塔顶回流泵（11）的出口端连通，减压脱轻塔（14）的出料口通过减压脱轻塔底泵（17）出料得到高碳醛产品；所述减压脱轻塔（14）的底部通过减压脱轻塔底再沸器（19）连接热源；The vacuum stripping tower (14) has an outlet at the top, a feed inlet on one side of the middle section, a discharge outlet at the bottom, and a reflux outlet on one side of the upper section. The feed inlet of the vacuum stripping tower (14) is connected to the outlet of the top reflux pump (11) of the vacuum stripping tower. The discharge outlet of the vacuum stripping tower (14) is discharged through the bottom pump (17) of the vacuum stripping tower to obtain high carbon aldehyde product. The bottom of the vacuum stripping tower (14) is connected to a heat source through the bottom reboiler (19) of the vacuum stripping tower. 减压脱轻塔顶回流罐（16）：减压脱轻塔顶回流罐（16）顶部设有进料口、出气口，底部设有出液口，减压脱轻塔顶回流罐（16）的进料口通过减压脱轻塔顶冷却器（15）与减压脱轻塔（14）的出气口连通，减压脱轻塔顶回流罐（16）的出气口与真空泵（6）的进口端连通，减压脱轻塔顶回流罐（16）的出液口通过减压脱轻塔顶回流泵（18）分别与减压脱轻塔（14）的回流口、烯烃/催化剂混合器（23）连通。Top reflux tank (16) of vacuum stripping light tower: The top reflux tank (16) of vacuum stripping light tower is provided with a feed inlet and an outlet, and a liquid outlet at the bottom. The feed inlet of the top reflux tank (16) of vacuum stripping light tower is connected to the outlet of vacuum stripping light tower (14) through the top cooler (15) of vacuum stripping light tower. The outlet of the top reflux tank (16) of vacuum stripping light tower is connected to the inlet of vacuum pump (6). The liquid outlet of the top reflux tank (16) of vacuum stripping light tower is connected to the reflux port of vacuum stripping light tower (14) and olefin/catalyst mixer (23) through the top reflux pump (18) of vacuum stripping light tower. 2.如权利要求1所述的高碳链烯烃氢甲酰化反应和分离的组合系统，其特征在于，所述减压脱重塔顶冷却器（8）、减压脱轻塔顶冷却器（15）的冷源均采用冷冻水。2. The combined system for hydroformylation reaction and separation of high-carbon chain olefins as described in claim 1, characterized in that the cold source for both the vacuum de-heavy tower top cooler (8) and the vacuum de-light tower top cooler (15) is chilled water. 3.如权利要求1所述的高碳链烯烃氢甲酰化反应和分离的组合系统，其特征在于，所述烯烃/催化剂混合器（23）的入口端前设有烯烃净化器（22）。3. The combined system for hydroformylation reaction and separation of high-carbon chain olefins as described in claim 1, characterized in that an olefin purifier (22) is provided before the inlet end of the olefin/catalyst mixer (23). 4.如权利要求1所述的高碳链烯烃氢甲酰化反应和分离的组合系统，其特征在于，所述合成气缓冲罐（20）的出气口依次设有合成气增压机（26）、合成气净化器（21）。4. The combined system for hydroformylation reaction and separation of high carbon chain olefins as described in claim 1, characterized in that the outlet of the syngas buffer tank (20) is provided with a syngas booster (26) and a syngas purifier (21) in sequence. 5.如权利要求1所述的高碳链烯烃氢甲酰化反应和分离的组合系统，其特征在于，所述减压脱重塔顶回流泵（11）与减压脱轻塔（14）进料口之间的管路、减压脱轻塔底泵（17）的出料管路通过减压脱轻塔进料换热器（13）进行换热。5. The combined system for hydroformylation reaction and separation of high carbon chain olefins as described in claim 1, characterized in that the pipeline between the top reflux pump (11) of the vacuum de-heavy tower and the feed inlet of the vacuum de-light tower (14), and the discharge pipeline of the bottom pump (17) of the vacuum de-light tower, exchange heat through the feed heat exchanger (13) of the vacuum de-light tower.
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