CN115430368A - System and process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing - Google Patents
System and process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing Download PDFInfo
- Publication number
- CN115430368A CN115430368A CN202211054029.9A CN202211054029A CN115430368A CN 115430368 A CN115430368 A CN 115430368A CN 202211054029 A CN202211054029 A CN 202211054029A CN 115430368 A CN115430368 A CN 115430368A
- Authority
- CN
- China
- Prior art keywords
- carbonylation
- gas
- liquid
- butyraldehyde
- reactor
- 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.)
- Pending
Links
Images
Classifications
-
- 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
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group
- C07C29/141—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group with hydrogen or hydrogen-containing gases
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/17—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
- C07C29/175—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds with simultaneous reduction of an oxo group
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- 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
- C07C45/505—Asymmetric hydroformylation
-
- 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
- C07C45/61—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups
- C07C45/67—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton
- C07C45/68—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms
- C07C45/72—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction of compounds containing >C = O groups with the same or other compounds containing >C = O groups
- C07C45/74—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction of compounds containing >C = O groups with the same or other compounds containing >C = O groups combined with dehydration
Abstract
The invention discloses a system and a process for preparing butanol and octanol through carbonylation slurry gas-liquid mixing and carbonylation slurry gas-liquid mixing, and relates to the technical field of carbonylation to synthesize butanol and octanol. The carbonylation slurry gas-liquid mixer is externally arranged at the bottom of the carbonylation reactor, and is used for fully crushing and mixing liquid-phase feeding materials and gas-phase feeding materials to form gas-liquid emulsion, increasing the gas-liquid contact area, increasing the phase interface area and the mass transfer rate of the reaction, improving the material conversion rate and the processing capacity of the reaction kettle, solving the problems of low system reaction efficiency caused by uneven mixing and by-product generation between the materials, realizing the yield improvement and consumption reduction of a butanol-octanol device, and improving the productivity and competitiveness of enterprises.
Description
Technical Field
The invention relates to the technical field of synthesizing butanol and octanol by a carbonyl method, in particular to a system and a process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing.
Background
The butanol and octanol are important raw materials for synthesizing fine chemical products, the yield of the butanol and octanol in China is huge at present and accounts for about 21% of the total amount of the world, the butanol and octanol take synthesis gas and propylene as raw materials, n-isobutyraldehyde is generated through a carbonyl reaction, then the n-isobutyraldehyde is obtained through a hydrogenation reaction, and the octanol can also be obtained through condensation of two molecules of n-butanol, regeneration and addition of an unsaturated bond, so that the butanol and octanol is custom-called. The butanol and octanol have the typical characteristics of alcohol organic matters, have special odors, are colorless, transparent and flammable liquids, have moderate toxicity and can form an azeotrope with water. The method is mainly used for producing plasticizers, solvents, dehydrating agents, defoaming agents, dispersing agents, flotation agents, petroleum additives, synthetic spices and the like. Due to the wide application, the yield and the dosage of the butanol and the octanol are also improved year by year.
The production products of some small and medium-sized enterprises are single, only butanol devices are contained, octanol products are not produced, the switching production of butanol and octanol cannot be carried out, and the risk resistance is weak. In the traditional production process of the butanol and the octanol, the propylene, the synthesis gas and the catalyst are not uniformly mixed in the oxo-synthesis reactor, by-products are generated, the reaction efficiency is low, and the competitive advantage is lacked in the fierce market environment. How to improve the productivity, the conversion rate of reaction materials and the processing capacity of the oxo reactor by improving the productivity is a main problem at present.
Disclosure of Invention
In order to solve the technical problems, the invention provides a system and a process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing, which optimize the traditional butanol and octanol production process. According to the invention, the raw material inlet of the oxo-synthesis reactor is provided with the carbonylation slurry gas-liquid mixer, so that the gas-liquid contact area is increased, the phase interface area and the mass transfer rate of the reaction are increased, the material conversion rate and the processing capacity of the reaction kettle are improved, the problem of low system reaction efficiency caused by uneven mixing and byproduct generation between materials is solved, the yield of the butanol-octanol device is increased, the consumption is reduced, and the productivity and the competitiveness of enterprises are improved.
In order to realize the purpose, the technical scheme of the invention is as follows:
in a first aspect, a system for preparing butanol and octanol by carbonylation slurry gas-liquid mixing comprises:
the carbonylation slurry gas-liquid mixer is used for fully crushing and mixing liquid-phase feeding materials and gas-phase feeding materials to form gas-liquid emulsion; the gas-liquid contact area is increased, the phase interface area and the mass transfer rate of the reaction are increased, and the material conversion rate and the treatment capacity of the reaction kettle are improved;
the carbonylation unit is connected with the carbonylation slurry gas-liquid mixer and is used for performing carbonylation on the material output by the carbonylation slurry gas-liquid mixer to form butyraldehyde;
a butyraldehyde refining unit connected with the oxo-synthesis unit and used for separating and removing the material output by the oxo-synthesis unit;
the butyraldehyde condensation unit is connected with the butyraldehyde refining unit and used for providing a reaction site for the output materials of the butyraldehyde refining unit and separating and removing the output materials;
the hydrogenation reaction unit is used for providing a reaction site for the output material of the butyraldehyde refining unit and hydrogen or providing a reaction site for the output material of the butyraldehyde condensation unit and hydrogen;
and the rectifying unit is connected with the hydrogenation reaction unit and is used for separating and purifying the material output by the hydrogenation reaction unit.
In a second aspect, a process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing adopts the system for preparing butanol and octanol by carbonylation slurry gas-liquid mixing; the method comprises the following steps:
step 1: delivering propylene into the oxo reactor through the propylene feed pipe, and delivering a catalyst into the carbonylation slurry gas-liquid mixer through the catalyst feed pipe; conveying the synthesis gas to a carbonylation slurry gas-liquid mixer through a synthesis gas pipeline;
and 2, step: the carbonylation slurry gas-liquid mixer is used for crushing the catalyst and the synthesis gas to form a gas-liquid emulsion, and after the catalyst and the synthesis gas are mixed, the carbonylation slurry gas-liquid mixer outputs the gas-liquid emulsion to the carbonylation reactor; carrying out carbonyl synthesis reaction on the gas-liquid emulsion and propylene under the action of a catalyst to generate a butyraldehyde mixture;
and 3, step 3: the method comprises the following steps of (1) separating a butyraldehyde mixture after entering a butyraldehyde isomerizator tower, selling the separated isobutyraldehyde as a product, conveying the separated n-butyraldehyde into a hydrogenation reactor, feeding hydrogen into the hydrogenation reactor along a hydrogen feeding pipeline, and carrying out hydrogenation reaction on the n-butyraldehyde and the hydrogen to produce a butanol mixture;
or conveying the separated n-butyraldehyde to a condensation reactor of a butyraldehyde condensation reaction unit, carrying out carbonyl condensation reaction on the n-butyraldehyde in the condensation reactor, conveying a reaction product to a hydrogenation reactor, and carrying out hydrogenation reaction on the reaction product and hydrogen to produce an octanol mixture;
and 4, step 4: and the gas-phase component output by the hydrogenation reactor enters the rectifying tower for rectification, and the gas-phase component of the purified butanol or octanol is output and stored in the storage tank.
The invention has the beneficial effects that:
the invention realizes the industrial application of the micro-mixing technology by arranging the carbonylation slurry gas-liquid mixer at the raw material inlet of the carbonylation reactor and adopting a gas-liquid external mixing method for the first time.
By using the gas-liquid mixer for carbonylation slurry, the phase interface area and the mass transfer rate of the reaction are increased by increasing the gas-liquid contact area, the material conversion rate and the processing capacity of the reaction kettle are improved, and the problems of low system reaction efficiency caused by uneven mixing of materials and generation of byproducts are solved; the emptying amount of the oxo reactor is reduced, the reaction rate is accelerated, and the reaction depth is increased; the propylene loss and the emptying amount in the production process of the butanol and octanol are reduced, the yield increase and consumption reduction of a butanol and octanol device are realized, and the capacity and the competitiveness of enterprises are improved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are included to illustrate an exemplary embodiment of the invention and not to limit the invention.
FIG. 1 is a schematic diagram of the connection of a carbonylation slurry gas-liquid mixer and an oxo reactor in a system for preparing butanol-octanol by carbonylation slurry gas-liquid mixing according to example 1 of the present invention.
The system comprises a carbonylation reactor 1, a carbonylation slurry gas-liquid mixer 2 and a liquid phase cooling circulation device heat exchanger 3.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
The invention provides a system and a process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing, which are provided by the invention in view of the facts that the existing medium and small enterprises have single product and weak risk resistance, and propylene, synthesis gas and a catalyst are not uniformly mixed in a carbonylation reactor in the traditional production process of butanol and octanol, and a reaction efficiency is low due to the generation of byproducts.
In an exemplary embodiment of the present invention, a system for preparing butanol and octanol by carbonylation slurry gas-liquid mixing is provided, which comprises:
the carbonylation slurry gas-liquid mixer is used for fully crushing and mixing liquid-phase feeding materials and gas-phase feeding materials to form gas-liquid emulsion; the gas-liquid contact area is increased, the phase interface area and the mass transfer rate of the reaction are increased, and the material conversion rate and the treatment capacity of the reaction kettle are improved;
the carbonylation unit is connected with the carbonylation slurry gas-liquid mixer and is used for carrying out carbonylation synthesis on the material output by the carbonylation slurry gas-liquid mixer to form butyraldehyde;
a butyraldehyde refining unit connected with the oxo synthesis unit and used for separating and removing the material output by the oxo synthesis unit;
the butyraldehyde condensation unit is connected with the butyraldehyde refining unit and used for providing a reaction site for the output materials of the butyraldehyde refining unit and separating and removing the output materials;
the hydrogenation reaction unit is used for providing a reaction site for the output material of the butyraldehyde refining unit and hydrogen or providing a reaction site for the output material of the butyraldehyde condensation unit and hydrogen;
and the rectifying unit is connected with the hydrogenation reaction unit and is used for separating and purifying the material output by the hydrogenation reaction unit.
The liquid-phase feeding of the invention is the feeding after the temperature reduction of the heat exchanger, and the temperature reduction of the heat exchanger does not need to be increased independently. When the liquid phase substance catalyst and the synthesis gas enter the carbonylation slurry gas-liquid mixer together, the liquid phase substance is crushed by the pressure of the synthesis gas, thereby forming micro bubbles and increasing the contact area.
The principle of the carbonylation slurry gas-liquid mixer is that the diameters of gas or liquid phase particles at gas-liquid, liquid-liquid and gas-liquid phase interfaces of a reaction system are crushed into micron-sized (40-850 mu m) ranges, so that the mass transfer area and the total mass transfer rate between gas-liquid and liquid-liquid can be increased exponentially, the reaction speed is greatly increased, side reactions are effectively controlled, the product yield is increased, the energy consumption and material consumption in the reaction process are obviously reduced, the safety of a reaction section is improved, and the like.
In some embodiments of this embodiment, the oxo unit comprises:
the carbonylation reactor is used for providing a reaction site for the material output by the carbonylation slurry gas-liquid mixer;
the liquid phase cooling and circulating device of the oxo reactor is used for reducing the temperature of a liquid phase in the oxo reactor, and comprises a pipeline, a pump, a valve and a heat exchanger; the bottom of the oxo reactor is connected with a valve for controlling a liquid phase to flow out from the bottom of the oxo reactor, the liquid phase of the oxo reactor is conveyed into a pump through a pipeline for pressurization, the pressurized liquid phase enters a heat exchanger for heat exchange and cooling to obtain cooling circulating liquid of the oxo reactor; cooling circulating liquid of the carbonylation reactor flows into a carbonylation slurry gas-liquid mixer through a pipeline;
a propylene feed conduit disposed in a sidewall of the oxo reactor for conveying propylene to the oxo reactor;
a catalyst feed pipe connected with a material inlet pipe of the carbonylation slurry gas-liquid mixer, for conveying the catalyst into the carbonylation slurry gas-liquid mixer, and crushing the catalyst and the gas phase into slurry;
the carbonylation slurry gas-liquid mixer is arranged outside the carbonylation reactor.
In some examples of this embodiment, the gas phase inlet of the carbonylation slurry gas-liquid mixer is connected to the synthesis gas, the synthesis gas is fed as the gas phase to the carbonylation slurry gas-liquid mixer, the liquid phase inlet of the carbonylation slurry gas-liquid mixer is connected to the liquid phase cooling circulation unit of the carbonylation reactor, the catalyst feed conduit, and the catalyst is fed as the liquid phase to the carbonylation slurry gas-liquid mixer.
In some examples of this embodiment, the feed outlet of the carbonylation slurry gas-liquid mixer is connected to the middle of the oxo reactor.
In some embodiments of this embodiment, the butyraldehyde refining unit comprises:
and the butyraldehyde isomerate tower is connected with the carbonyl synthesis unit and is used for separating butyraldehyde in the output material of the hydroxyl synthesis unit.
In some embodiments of this embodiment, the butyraldehyde condensation unit comprises:
and the condensation reactor is connected with the butyraldehyde refining unit and is used for providing a reaction site for condensation reaction of the output materials of the butyraldehyde refining unit.
In some embodiments of this embodiment, the hydrogenation reaction unit comprises:
the hydrogenation reactor is used for providing a reaction site for the output material of the butyraldehyde refining unit and hydrogen, or is used for providing a reaction site for the output material of the butyraldehyde condensation unit and hydrogen;
the hydrogen feeding pipeline is arranged in the middle of the hydrogenation reactor and is used for conveying hydrogen into the hydrogenation reactor;
the feeding pipeline 1 is connected with the butyraldehyde refining unit and is used for conveying an output material of the butyraldehyde refining unit into the hydrogenation reactor;
and the feeding pipeline 2 is connected with the butyraldehyde condensation unit and is used for conveying the output material of the butyraldehyde condensation unit to the hydrogenation reactor.
In some embodiments of this embodiment, the rectification unit comprises:
the rectifying tower is connected with the hydrogenation reaction unit and is used for rectifying and purifying the material output by the hydrogenation reaction unit;
and the storage tank is connected with the rectifying tower and is used for storing the material output by the rectifying tower.
The invention provides a process for preparing butanol by carbonylation slurry gas-liquid mixing, which adopts the system for preparing butanol by carbonylation slurry gas-liquid mixing described in the first exemplary embodiment; the method comprises the following steps:
step 1: delivering propylene into the oxo reactor through the propylene feed pipe, and delivering a catalyst into the carbonylation slurry gas-liquid mixer through the catalyst feed pipe; conveying the synthesis gas to a carbonylation slurry gas-liquid mixer through a synthesis gas pipeline;
step 2: the carbonylation slurry gas-liquid mixer is used for crushing the catalyst and the synthesis gas to form a gas-liquid emulsion, and after the catalyst and the synthesis gas are mixed, the carbonylation slurry gas-liquid mixer outputs the gas-liquid emulsion to the carbonylation reactor; carrying out carbonyl synthesis reaction on the gas-liquid emulsion and propylene under the action of a catalyst to generate a butyraldehyde mixture;
and 3, step 3: the method comprises the following steps of (1) separating a butyraldehyde mixture after entering a butyraldehyde isomerizator tower, selling the separated isobutyraldehyde as a product, conveying the separated n-butyraldehyde into a hydrogenation reactor, feeding hydrogen into the hydrogenation reactor along a hydrogen feeding pipeline, and carrying out hydrogenation reaction on the n-butyraldehyde and the hydrogen to produce a butanol mixture;
or the separated n-butyraldehyde is conveyed into a condensation reactor of a butyraldehyde condensation reaction unit, the n-butyraldehyde is subjected to carbonyl condensation reaction in the condensation reactor, and a reaction product is conveyed into a hydrogenation reactor and subjected to hydrogenation reaction with hydrogen to produce an octanol mixture;
and 4, step 4: and the gas-phase component output by the hydrogenation reactor enters the rectifying tower for rectification, and the gas-phase component of purified butanol or octanol is output and stored in the storage tank.
In some examples of this embodiment, the reaction temperature in the oxo reactor in the process is between 80 ℃ and 100 ℃ and the reaction pressure is between 1.5 MPa and 2.0MPa.
Preferably, in the process, the reaction temperature in the oxo reactor is 85-92 ℃ and the reaction pressure is 1.65-1.83MPa.
In order to make the technical solutions of the present invention more clearly understood by those skilled in the art, the technical solutions of the present invention will be described in detail below with reference to specific embodiments.
Example 1
A system for preparing butanol and octanol by carbonylation slurry gas-liquid mixing sequentially comprises the following components in the material flow direction: the device comprises a carbonylation slurry gas-liquid mixer, a carbonylation synthesis unit, a butyraldehyde refining unit, a butyraldehyde condensation unit, a hydrogenation reaction unit and a rectification unit.
The oxo-synthesis unit comprises an oxo-synthesis reactor, a liquid-phase cooling circulation device of the oxo-synthesis reactor, a propylene feed pipeline and a catalyst feed pipeline.
The butyraldehyde refining unit comprises butyraldehyde isomers.
The butyraldehyde condensation unit comprises a condensation reactor.
The hydrogenation reaction unit comprises a hydrogenation reactor, a hydrogen feeding pipeline, a feeding pipeline 1 and a feeding pipeline 2.
The rectifying unit comprises a rectifying tower and a storage tank in sequence according to the material flow direction.
The carbonylation slurry gas-liquid mixer is arranged outside the carbonylation synthesis reactor, the gas phase inlet of the carbonylation slurry gas-liquid mixer is connected with the synthesis gas, the synthesis gas is used as the gas phase feeding of the carbonylation slurry gas-liquid mixer, the liquid phase inlet of the micro-interface strengthening reactor is connected with the liquid phase cooling circulation device of the carbonylation synthesis reactor, and the catalyst is used as the liquid phase feeding of the carbonylation slurry gas-liquid mixer. The material outlet of the carbonylation slurry gas-liquid mixer is connected with the middle part of the carbonylation reactor.
The material outlet of the oxo reactor is connected with the material inlet of the butyraldehyde isomeride tower, and the butyraldehyde mixture synthesized in the oxo reactor is separated by the butyraldehyde isomeride tower to separate n-butyraldehyde and isobutyraldehyde. The n-butyraldehyde is transported to the hydrogenation reactor through a feed line 1, or to the condensation reactor through a feed line 2. The material outlet of the condensation reactor is connected with the hydrogenation reactor.
The material outlet of the hydrogenation reactor is connected with the material inlet of the rectifying tower, and the material outlet of the rectifying tower is connected with the storage tank.
Wherein, the liquid phase cooling circulation device of the oxo reactor is used for reducing the temperature of the liquid phase in the oxo reactor and comprises a pipeline, a pump, a valve and a heat exchanger; the bottom of the oxo reactor is connected with a valve for controlling a liquid phase to flow out from the bottom of the oxo reactor, the liquid phase of the oxo reactor is conveyed into a pump through a pipeline for pressurization, the pressurized liquid phase enters a heat exchanger for heat exchange and cooling to obtain cooling circulating liquid of the oxo reactor; the cooling circulating liquid of the carbonylation reactor flows into a carbonylation slurry gas-liquid mixer through a pipeline.
Example 2
A process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing adopts the system for preparing butanol and octanol by carbonylation slurry gas-liquid mixing in the embodiment 1;
a process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing comprises the following steps:
step 1: delivering propylene into the oxo reactor through the propylene feed pipe, and delivering a catalyst into the carbonylation slurry gas-liquid mixer through the catalyst feed pipe; conveying the synthesis gas to a carbonylation slurry gas-liquid mixer through a synthesis gas pipeline;
step 2: the carbonylation slurry gas-liquid mixer is used for crushing the catalyst and the synthesis gas to form a gas-liquid emulsion, and after the catalyst and the synthesis gas are mixed, the carbonylation slurry gas-liquid mixer outputs the gas-liquid emulsion to the carbonylation reactor; carrying out a oxo-synthesis reaction on the gas-liquid emulsion and propylene under the action of a catalyst to generate a butyraldehyde mixture;
and step 3: the method comprises the following steps of (1) separating a butyraldehyde mixture after entering a butyraldehyde isomerizator tower, selling the separated isobutyraldehyde as a product, conveying the separated n-butyraldehyde into a hydrogenation reactor, feeding hydrogen into the hydrogenation reactor along a hydrogen feeding pipeline, and carrying out hydrogenation reaction on the n-butyraldehyde and the hydrogen to produce a butanol mixture;
or the separated n-butyraldehyde is conveyed into a condensation reactor of a butyraldehyde condensation reaction unit, the n-butyraldehyde is subjected to carbonyl condensation reaction in the condensation reactor, and a reaction product is conveyed into a hydrogenation reactor and subjected to hydrogenation reaction with hydrogen to produce an octanol mixture;
and 4, step 4: and the gas-phase component output by the hydrogenation reactor enters the rectifying tower for rectification, and the gas-phase component of the purified butanol or octanol is output and stored in the storage tank.
In the process, the reaction temperature in the oxo reactor is 85-92 ℃, and the reaction pressure is 1.65-1.83MPa.
In the embodiment, the emptying amount of the oxo reactor is reduced by 10-20%, the reaction rate is accelerated, and the reaction depth is increased; the propylene loss and the air release amount in the butanol production process are reduced by 10-25%, the yield of a butanol device is increased by 10-15%, and the productivity and the competitiveness of an enterprise are improved.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A system for preparing butanol and octanol by carbonylation slurry gas-liquid mixing is characterized by comprising the following components:
the carbonylation slurry gas-liquid mixer is used for fully crushing and mixing liquid-phase feeding materials and gas-phase feeding materials to form gas-liquid emulsion; the gas-liquid contact area is increased, the phase interface area and the mass transfer rate of the reaction are increased, and the material conversion rate and the treatment capacity of the reaction kettle are improved;
the carbonylation unit is connected with the carbonylation slurry gas-liquid mixer and is used for carrying out carbonylation synthesis on the material output by the carbonylation slurry gas-liquid mixer to form butyraldehyde;
a butyraldehyde refining unit connected with the oxo synthesis unit and used for separating and removing the material output by the oxo synthesis unit;
the butyraldehyde condensation unit is connected with the butyraldehyde refining unit and used for providing a reaction site for the output materials of the butyraldehyde refining unit and separating and removing the output materials;
the hydrogenation reaction unit is used for providing a reaction site for the output material of the butyraldehyde refining unit and hydrogen or providing a reaction site for the output material of the butyraldehyde condensation unit and hydrogen;
and the rectifying unit is connected with the hydrogenation reaction unit and is used for separating and purifying the material output by the hydrogenation reaction unit.
2. The system for carbonylation slurry gas-liquid mixing to produce butanol-octanol of claim 1, wherein the oxo unit comprises:
the carbonylation reactor is used for providing a reaction site for the material output by the carbonylation slurry gas-liquid mixer;
the liquid phase cooling and circulating device of the oxo reactor is used for reducing the temperature of a liquid phase in the oxo reactor and comprises a pipeline, a pump, a valve and a heat exchanger; the bottom of the oxo reactor is connected with a valve for controlling a liquid phase to flow out from the bottom of the oxo reactor, the liquid phase of the oxo reactor is conveyed into a pump through a pipeline for pressurization, the pressurized liquid phase enters a heat exchanger for heat exchange and cooling to obtain cooling circulating liquid of the oxo reactor; cooling circulating liquid of the carbonylation reactor flows into a carbonylation slurry gas-liquid mixer through a pipeline;
a propylene feed conduit disposed in a sidewall of the oxo reactor for conveying propylene to the oxo reactor;
a catalyst feeding pipeline which is connected with a material inlet pipeline of the carbonylation slurry gas-liquid mixer and is used for conveying the catalyst into the carbonylation slurry gas-liquid mixer and crushing the catalyst into a slurry state together with a gas phase;
the carbonylation slurry gas-liquid mixer is arranged outside the carbonylation reactor.
3. The carbonylation slurry gas-liquid mixing butanol-octanol production system according to claim 2, wherein the gas phase inlet of said carbonylation slurry gas-liquid mixer is connected to the synthesis gas as the gas phase feed to said carbonylation slurry gas-liquid mixer, the liquid phase inlet of said carbonylation slurry gas-liquid mixer is connected to the liquid phase cooling circulation unit of said carbonylation synthesis reactor, the catalyst feed conduit, and the catalyst is the liquid phase feed to said carbonylation slurry gas-liquid mixer.
4. The carbonylation slurry gas-liquid mixing butanol-octanol production system of claim 2, wherein the feed outlet of the carbonylation slurry gas-liquid mixer is connected to the middle of the oxo reactor.
5. The system for preparing butanol-octanol by carbonylation of slurry gas-liquid mixture according to claim 1, wherein said butyraldehyde refining unit comprises:
and the butyraldehyde isomerate tower is connected with the carbonyl synthesis unit and is used for separating butyraldehyde in the output material of the hydroxyl synthesis unit.
6. The carbonylation slurry gas-liquid mixing butanol-octanol system according to claim 1, wherein the butyraldehyde condensation unit comprises:
and the condensation reactor is connected with the butyraldehyde refining unit and is used for providing a reaction site for condensation reaction of the output materials of the butyraldehyde refining unit.
7. The system for preparing butanol-octanol by carbonylation slurry gas-liquid mixing according to claim 1, wherein the hydrogenation reaction unit comprises:
the hydrogenation reactor is used for providing a reaction site for the output material of the butyraldehyde refining unit and hydrogen, or is used for providing a reaction site for the output material of the butyraldehyde condensation unit and hydrogen;
the hydrogen feeding pipeline is arranged in the middle of the hydrogenation reactor and is used for conveying hydrogen into the hydrogenation reactor;
the feeding pipeline 1 is connected with the butyraldehyde refining unit and is used for conveying an output material of the butyraldehyde refining unit into the hydrogenation reactor;
and the feeding pipeline 2 is connected with the butyraldehyde condensation unit and is used for conveying the output material of the butyraldehyde condensation unit into the hydrogenation reactor.
8. The system for preparing butanol-octanol by carbonylation of slurry gas-liquid mixing according to claim 1, wherein said rectification unit comprises:
the rectifying tower is connected with the hydrogenation reaction unit and is used for rectifying and purifying the material output by the hydrogenation reaction unit;
and the storage tank is connected with the rectifying tower and is used for storing the material output by the rectifying tower.
9. A process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing, which is characterized in that the system for preparing butanol and octanol by carbonylation slurry gas-liquid mixing of any one of claims 1-8 is adopted; the method comprises the following steps:
step 1: delivering propylene into the oxo reactor through the propylene feed pipe, and delivering a catalyst into the carbonylation slurry gas-liquid mixer through the catalyst feed pipe; conveying the synthesis gas to a carbonylation slurry gas-liquid mixer through a synthesis gas pipeline;
step 2: the carbonylation slurry gas-liquid mixer is used for crushing the catalyst and the synthesis gas to form a gas-liquid emulsion, and after the catalyst and the synthesis gas are mixed, the carbonylation slurry gas-liquid mixer outputs the gas-liquid emulsion to the carbonylation reactor; carrying out a oxo-synthesis reaction on the gas-liquid emulsion and propylene under the action of a catalyst to generate a butyraldehyde mixture;
and 3, step 3: the method comprises the following steps of (1) separating a butyraldehyde mixture after entering a butyraldehyde isomerizator tower, selling the separated isobutyraldehyde as a product, conveying the separated n-butyraldehyde into a hydrogenation reactor, feeding hydrogen into the hydrogenation reactor along a hydrogen feeding pipeline, and carrying out hydrogenation reaction on the n-butyraldehyde and the hydrogen to produce a butanol mixture;
or conveying the separated n-butyraldehyde to a condensation reactor of a butyraldehyde condensation reaction unit, carrying out carbonyl condensation reaction on the n-butyraldehyde in the condensation reactor, conveying a reaction product to a hydrogenation reactor, and carrying out hydrogenation reaction on the reaction product and hydrogen to produce an octanol mixture;
and 4, step 4: and the gas-phase component output by the hydrogenation reactor enters the rectifying tower for rectification, and the gas-phase component of purified butanol or octanol is output and stored in the storage tank.
10. The process for preparing butanol-octanol by carbonylation slurry gas-liquid mixing and carbonylation slurry gas-liquid mixing as claimed in claim 9, wherein in the process, the reaction temperature in the oxo reactor is 80-100 ℃, and the reaction pressure is 1.5-2.0MPa;
preferably, in the process, the reaction temperature in the oxo reactor is 85-92 ℃ and the reaction pressure is 1.65-1.83MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211054029.9A CN115430368A (en) | 2022-08-31 | 2022-08-31 | System and process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211054029.9A CN115430368A (en) | 2022-08-31 | 2022-08-31 | System and process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115430368A true CN115430368A (en) | 2022-12-06 |
Family
ID=84244529
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211054029.9A Pending CN115430368A (en) | 2022-08-31 | 2022-08-31 | System and process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115430368A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116272815A (en) * | 2023-05-17 | 2023-06-23 | 江苏省瑞丰高分子材料有限公司 | Quick switching device of reaction kettle and rectifying tower |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB747493A (en) * | 1952-06-07 | 1956-04-04 | Exxon Research Engineering Co | Improved oxo aldehyde synthesis |
| CN104801249A (en) * | 2015-04-01 | 2015-07-29 | 中石化上海工程有限公司 | Method for recycling energy in oxo synthesis device |
| CN112010735A (en) * | 2020-08-18 | 2020-12-01 | 南京延长反应技术研究院有限公司 | External micro-interface strengthening system and method for preparing butanol and octanol through propylene carbonylation |
| CN112479815A (en) * | 2019-09-12 | 2021-03-12 | 南京延长反应技术研究院有限公司 | Reaction system and process for preparing butanol and octanol through propylene carbonylation based on micro-interface reinforcement |
-
2022
- 2022-08-31 CN CN202211054029.9A patent/CN115430368A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB747493A (en) * | 1952-06-07 | 1956-04-04 | Exxon Research Engineering Co | Improved oxo aldehyde synthesis |
| CN104801249A (en) * | 2015-04-01 | 2015-07-29 | 中石化上海工程有限公司 | Method for recycling energy in oxo synthesis device |
| CN112479815A (en) * | 2019-09-12 | 2021-03-12 | 南京延长反应技术研究院有限公司 | Reaction system and process for preparing butanol and octanol through propylene carbonylation based on micro-interface reinforcement |
| CN112010735A (en) * | 2020-08-18 | 2020-12-01 | 南京延长反应技术研究院有限公司 | External micro-interface strengthening system and method for preparing butanol and octanol through propylene carbonylation |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116272815A (en) * | 2023-05-17 | 2023-06-23 | 江苏省瑞丰高分子材料有限公司 | Quick switching device of reaction kettle and rectifying tower |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2021047042A1 (en) | Reaction system and process for preparing butanol and octanol based on microinterface-enhanced carbonylation of propylene | |
| CN210176754U (en) | Catalyst-free oxidation strengthening system for cyclopentane | |
| CN104250205B (en) | The preparation method of methyl tertiary butyl ether and device thereof | |
| CN111302917B (en) | Olefin hydroformylation device and method | |
| CN101735047A (en) | Technology for continuously producing secbutyl acetate | |
| WO2023138074A1 (en) | Method and system for preparing cyclic carbonate by catalyzing carbon dioxide cycloaddition | |
| CN107056582A (en) | Coal-ethylene glycol carbonylation system reclaims the system and method for methyl nitrite | |
| CN115430368A (en) | System and process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing | |
| CN104557478A (en) | Method for preparing tert-butyl ether | |
| CN111689845B (en) | Process for producing succinic acid by maleic anhydride aqueous phase hydrogenation | |
| CN205188177U (en) | Methyl nitrite's regenerating unit system in synthetic gas system ethylene glycol technology | |
| CN106278836A (en) | Intermediate concentration formaldehyde and the apparatus and method of methylal synthesis polymethoxy dimethyl ether | |
| CN114702375B (en) | Separation system and method for acetaldehyde product prepared from ethanol | |
| CN104311513A (en) | Method of preparing propylene epoxide | |
| CN101456849B (en) | Method and apparatus for preparing epoxypropane by catalyzing propone epoxidation at supercritical condition | |
| CN107628929A (en) | A kind of production technology of the propane diols of hydrogenolysis of glycerin system 1,2 | |
| CN210674823U (en) | Wash oil and direct liquefied coal oil mixed processing system | |
| CN109928943B (en) | Method for synthesizing propylene oxide by using microchannel reactor | |
| WO2020155506A1 (en) | Bottom-mounted gas-liquid enhanced emulsification fixed-bed reaction device and method | |
| CN214598924U (en) | Micro-interface preparation device of butanol and octanol | |
| CN104829435A (en) | Apparatus for producing MTBE by using novel catalytic distillation structured packing, and method thereof | |
| CN110551002A (en) | Method for preparing tert-butyl alcohol by hydrating carbon tetraisobutylene component and preparation system thereof | |
| WO2020155504A1 (en) | Side-arranged type residual oil hydrogenation emulsification bed micro-interface enhanced reaction device and method | |
| CN112574021A (en) | Enhanced carbonylation reaction system and process | |
| CN219291366U (en) | System for preparing cyclohexene by cyclohexane dehydrogenation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |