CN113813879B - Evaporation mixer and methylamine synthesis device - Google Patents

Evaporation mixer and methylamine synthesis device Download PDF

Info

Publication number
CN113813879B
CN113813879B CN202111000732.7A CN202111000732A CN113813879B CN 113813879 B CN113813879 B CN 113813879B CN 202111000732 A CN202111000732 A CN 202111000732A CN 113813879 B CN113813879 B CN 113813879B
Authority
CN
China
Prior art keywords
methylamine
evaporation
product
mixer
steam
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN202111000732.7A
Other languages
Chinese (zh)
Other versions
CN113813879A (en
Inventor
郑可嘉
陈峰华
刘立新
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Beijing Xinmeige Engineering Design Co ltd
Original Assignee
Beijing Xinmeige Engineering Design Co ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Beijing Xinmeige Engineering Design Co ltd filed Critical Beijing Xinmeige Engineering Design Co ltd
Priority to CN202111000732.7A priority Critical patent/CN113813879B/en
Publication of CN113813879A publication Critical patent/CN113813879A/en
Application granted granted Critical
Publication of CN113813879B publication Critical patent/CN113813879B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/008—Feed or outlet control devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0011—Heating features
    • B01D1/0041—Use of fluids
    • B01D1/0047—Use of fluids in a closed circuit
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0082—Regulation; Control
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/30—Accessories for evaporators ; Constructional details thereof
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • 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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/04—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of functional groups by amino groups
    • C07C209/14—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of functional groups by amino groups by substitution of hydroxy groups or of etherified or esterified hydroxy groups
    • C07C209/16—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of functional groups by amino groups by substitution of hydroxy groups or of etherified or esterified hydroxy groups with formation of amino groups bound to acyclic carbon atoms or to carbon atoms of rings other than six-membered aromatic rings
    • 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
    • B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
    • B01J2204/002—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the feeding side being of particular interest
    • 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
    • B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
    • B01J2204/005—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the outlet side being of particular interest
    • 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
    • B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
    • B01J2204/007—Aspects relating to the heat-exchange of the feed or outlet devices
    • 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
    • Y02P20/10—Process efficiency
    • 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
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention provides an evaporation mixer and a methylamine synthesizing device, wherein the evaporation mixer comprises: the horizontal type shell is internally and oppositely provided with a steam evaporator and a product heat exchanger; the steam evaporator comprises a heating tube bundle and a steam feeding and discharging end socket, and the product heat exchanger comprises a heat exchange tube bundle and a product feeding and discharging end socket; and (3) enabling the methylamine product to enter the horizontal shell so as to recover the heat of the methylamine product. The evaporation mixer disclosed by the invention can effectively reduce the equipment occupation area of an evaporation mixing system, reduces the overall height of the evaporation mixing equipment, and is convenient to install on site while reducing the energy consumption of conveying equipment. The methylamine synthesis device can reduce the energy consumption of unit products, improve the yield of dimethylamine, reduce the operation load of a downstream product separation system on the premise of improving the product competitiveness, and lay a foundation for saving energy consumption and material consumption of subsequent rectification separation.

Description

Evaporation mixer and methylamine synthesis device
Technical Field
The invention relates to the technical field of chemical production, in particular to an evaporation mixer and a methylamine synthesizing device.
Background
Methylamine is an important basic organic chemical raw material, is widely applied to various industries of national economy, and is a basic raw material for industries such as pesticides, medicines, synthetic dyes, synthetic resins, chemical fibers, solvents, surfactants, high-energy fuels, photographic materials and the like.
Methylamine is divided into monomethylamine, dimethylamine and trimethylamine, and is generally produced by a gas-phase catalytic reaction method of methanol and ammonia in industry, wherein the method takes methanol and liquid ammonia as raw materials and adopts the gas-phase catalytic reaction to prepare the methylamine, and the main reactions are as follows:
CH3OH+NH3→CH3NH2+H2O+Q
2CH3OH+NH3→(CH3)2NH+2H2O+Q
3CH3OH+NH3→(CH3)3N+3H2O+Q
the method has rich raw material sources, low price, large-scale continuous production, lower requirements on equipment and materials, easy satisfaction of process conditions, flexible adjustment of the product proportion of the three types of methylamine according to market demands, and is also the most common production method in the current methylamine industry, and the current methylamine factories in China all adopt the process to produce methylamine.
In the method, liquid methanol, liquid circulating material and liquid ammonia are adopted as raw materials, a plurality of heat exchangers and vertical containers are adopted during feeding, the raw materials are connected through pipelines to form an evaporation mixing system of the raw materials, the raw materials methanol and the liquid ammonia are gasified, and the gasified materials are introduced into a reactor for reaction.
The existing evaporation mixing system has the disadvantages of large equipment quantity, large occupied space and high installation height, which causes higher energy consumption of conveying equipment; and the heat emitted after the gas-phase catalytic reaction is not effectively utilized in the evaporation mixing process, so that the direct loss of heat and the waste of energy are caused, the cost of unit products is indirectly improved through energy consumption, and the market competitiveness is reduced.
Disclosure of Invention
The invention aims to provide an evaporation mixer and a methylamine synthesis device, which can reduce equipment for preheating and mixing raw materials, simplify the feeding process, fully recover heat released after gas-phase catalytic reaction, and fundamentally reduce the energy consumption and production cost of unit methylamine products.
The invention provides an evaporative mixer, comprising: the horizontal shell is provided with a horizontal shell,
a steam evaporator and a product heat exchanger are oppositely arranged in the horizontal shell;
the steam evaporator comprises a heating tube bundle and a steam feeding and discharging end socket, and the product heat exchanger comprises a heat exchange tube bundle and a product feeding and discharging end socket;
and the methylamine product enters the horizontal shell so as to recover the heat of the methylamine product.
Furthermore, the horizontal shell comprises a mixing chamber for mixing and heating the raw materials, and the heating tube bundle and the heat exchange tube bundle are both arranged in the mixing chamber.
Furthermore, the steam feeding and discharging seal head and the product feeding and discharging seal head are both one and are respectively arranged at two ends of the horizontal shell.
Further, the heating tube bundle and the heat exchange tube bundle are both U-shaped tube bundles.
Further, the horizontal shell still includes and is located the evaporation chamber at mixing chamber top, the evaporation chamber with mixing chamber intercommunication, install in the evaporation chamber and be used for carrying out the demister that removes the foam to evaporating gas.
The utility model provides an including above-mentioned evaporation mixer's methylamine synthesizer, the methylamine synthetic raw materials among the evaporation mixer enters into the methylamine reactor after reheating and carries out the synthetic reaction, be provided with multistage catalytic unit in the methylamine reactor, every section catalytic unit is including the balanced type catalyst layer that is located the upper portion to and the molecular sieve catalyst layer that is located the lower part.
Further, the components of the equilibrium catalyst are respectively as follows by mass fraction: SiO 2215 to 30 parts of Al2O370-85 parts of a solvent; the molecular sieve catalyst comprises the following components in percentage by mass: SiO 2210 to 20 parts of Al2O340-60 parts of aluminosilicate and 40-50 parts of aluminosilicate.
Further, the volume ratio of the equilibrium catalyst to the molecular sieve catalyst is as follows: (2-3): 1.
in addition, the volume ratio between the two may also be 2.1:1, 2.2:1, 2.3:1, 2.4:1, 2.5:1, 2.6:1, 2.7:1, 2.8:1, 2.9:1, etc. The two catalysts are used for synergism to ensure the conversion rate of raw materials and the selectivity of dimethylamine of the reaction, so that the two indexes reach the optimal range to ensure the highest yield of the dimethylamine, the volume ratio is also obtained by practical optimization and needs to be controlled in an appropriate range, and if the volume ratio is too large or too small, the conversion rate or the selectivity of the dimethylamine cannot be ensured.
Further, still including carrying out reheating unit of reheating, reheating unit is including steam heater, raw materials pre-heater and the electric heater that sets gradually, steam heater's feed inlet with evaporation mixer's discharge gate is connected, electric heater's discharge gate with the feed inlet of methylamine reactor is connected.
Furthermore, the raw material preheater comprises a shell pass inlet and a shell pass outlet, the shell pass inlet is connected with a discharge port of the methylamine reactor, and the shell pass outlet is connected with a feed port of the product heat exchanger.
Furthermore, a circulating material tank and a methanol raw material tank are arranged at the upstream of the evaporation mixer, and circulating materials and methanol are respectively fed into the evaporation mixer through a circulating material feeding pump and a methanol feeding pump.
Further, still include the ammonia inlet pipe, the evaporation blender reaches be provided with the ammonia feed inlet on the methylamine reactor respectively, the ammonia passes through the ammonia feed inlet lets in respectively the evaporation blender reaches the methylamine reactor.
According to the evaporation mixer, the steam evaporator and the product heat exchanger are integrated on the evaporation mixer, so that the occupied area of the evaporation mixing system can be effectively reduced, the overall height of the evaporation mixing device is reduced, and the energy consumption of the conveying device is reduced and the on-site installation is facilitated.
Through letting in the methylamine product in the product heat exchanger that sets up in the evaporation mixer, can make the methylamine product that has a large amount of reaction heats carry out the heat transfer through the reaction raw materials in heat exchange tube bank and the mixing chamber, make the heat that the reaction generated obtain recycle in the mixed evaporation link of raw materials, effectively reduceed the energy consumption and the manufacturing cost of unit product, greatly improved product competitiveness.
The molecular sieve catalyst layer included in the methylamine reactor can further react trimethylamine with ammonia gas in a form of adsorbing the generated product by the molecular sieve, so that the conversion rate of the dimethylamine is effectively improved.
Through the methylamine synthesis device comprising the evaporation mixer and the methylamine reactor, the energy consumption of unit products can be reduced, the yield of dimethylamine can be improved, the operation load of a downstream product separation system can be reduced on the premise of improving the product competitiveness, and a foundation is laid for saving energy consumption and material consumption of subsequent rectification separation.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a schematic view of an evaporative mixer according to the present invention;
FIG. 2 is a process flow diagram of a methylamine production system of the present invention.
In the figure: 1-an evaporative mixer; 10-a horizontal shell; 11-a steam evaporator; 12-product heat exchanger; 111-a heating tube bundle; 121-a heat exchange tube bundle; 112-steam feeding and discharging end sockets; 122-product feeding and discharging end socket; 13-a mixing chamber; 14-an evaporation chamber; 141-a demister;
a 2-methylamine reactor; 20-a catalytic unit; 21-equilibrium catalyst layer; 22-a molecular sieve catalyst layer;
3-circulating the material tank; 31-circulating material feed pump;
4-a methanol feed tank; 41-methanol feed pump;
5-a steam heater; 6-raw material preheater; 7-electric heater.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings or the orientations or positional relationships that the products of the present invention are conventionally placed in use, and are only used for convenience in describing the present invention and simplifying the description, but do not indicate or imply that the devices or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
Furthermore, the terms "horizontal", "vertical", "overhang" and the like do not imply that the components are required to be absolutely horizontal or overhang, but may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Some embodiments of the invention are described in detail below with reference to the accompanying drawings. The embodiments described below and the features of the embodiments can be combined with each other without conflict.
Example 1
Referring to fig. 1, the evaporative mixer 1 provided in this embodiment includes: the horizontal-type shell body (10),
a steam evaporator 11 and a product heat exchanger 12 are oppositely arranged in the horizontal shell 10;
the steam evaporator 11 comprises a heating tube bundle 111 and a steam feed and discharge head 112, and the product heat exchanger 12 comprises a heat exchange tube bundle 121 and a product feed and discharge head 122;
the methylamine product enters the horizontal housing 10 to recover heat from the methylamine product.
The evaporation mixer 1 of the invention mainly mixes and evaporates the synthetic raw materials of methylamine, so that the fed methanol, liquid ammonia and circulating materials are evaporated and mixed in the evaporation mixer 1, and then the mixture is further heated and enters the methylamine reactor 2 for reaction.
The steam evaporator 11 and the product heat exchanger 12 are integrated on the horizontal shell 10 of the evaporation mixer 1 to form the double-heat-source pool-type evaporation mixer 1, so that methanol, liquid ammonia and circulating materials can be vaporized and evaporated in the same pool-type evaporation mixer 1, the equipment number of an evaporation system is reduced, the flows of raw materials in feeding and gasification are simplified, and the equipment investment cost is reduced.
The double heat source heat exchanger formed by the steam evaporator 11 and the product heat exchanger 12 which are oppositely arranged can recover reaction heat generated in the synthesis of the methylamine product in the pool type evaporation mixer 1 on the basis of the existing steam heating evaporation.
The steam evaporator 11 and the product heat exchanger 12 respectively include a heating tube bundle 111 and a heat exchange tube bundle 121 which are arranged inside the horizontal shell 10, steam enters the heating tube bundle 111 through the steam inlet and outlet end socket 112, and methylamine products enter the heat exchange tube bundle 121 through the product inlet and outlet end socket 122, so that the raw materials in the horizontal shell 10 of the evaporation mixer 1 are heated through the steam and the methylamine products carrying a large amount of reaction heat.
The steam inlet and outlet seal head 112 is provided with a steam inlet and a steam outlet, steam enters the heating tube bundle 111 from the steam inlet through the steam inlet and outlet seal head 112, and is converted into steam condensate after heating and evaporating the raw material in the horizontal shell 10 in the heating tube bundle 111, and the steam condensate is discharged from the steam evaporator 11 through the steam outlet.
The product inlet and outlet end enclosure 122 is provided with a product inlet and a product outlet, methylamine products return to the product heat exchanger 12 after being generated in the methylamine reactor 2, enter the heat exchange tube bundle 121 from the product inlet through the product inlet and outlet end enclosure 122, are discharged from the product heat exchanger 12 through the product outlet after heat exchange and evaporation are carried out on raw materials in the horizontal shell 10 in the heat exchange tube bundle 121, enter a downstream separation device for further treatment, and the methylamine products transfer reaction heat carried by the methylamine products to the raw materials in a heat exchange process in a heat conduction mode, and carry out evaporation and heat exchange on the raw materials while being cooled.
By passing the methylamine product through the heat exchange tube bundle 121 in the horizontal shell 10, a large amount of reaction heat released during the synthesis of methylamine is effectively recycled, and the energy consumption loss is reduced. Through the form of integrating the heater on horizontal casing 10, effectively reduced the equipment quantity and the whole equipment height of evaporation hybrid system, reduced conveying equipment's consumption to the equipment area of evaporation hybrid system has been reduced, the installation at the scene is do benefit to more.
Specifically, the raw material in the present embodiment is mixed and heated in the mixing chamber 13 in the horizontal shell 10, the heating tube bundle 111 and the heat exchange tube bundle 121 are both disposed in the mixing chamber 13, and preferably, the heating tube bundle 111 and the heat exchange tube bundle 121 are disposed below the liquid level of the mixed raw material. Through this kind of mode of setting, can make the heat in steam and the methylamine product fully shift to the liquid raw materials in, improved the evaporation efficiency of raw materials.
The steam evaporator 11 and the product heat exchanger 12 both include a single-ended head, that is, the steam inlet/outlet head 112 and the product inlet/outlet head 122 are both one and respectively disposed at two ends of the horizontal housing 10. Through connecting the tube bank on the closing head to make the outside pipeline connection who carries steam and product on the closing head, be favorable to the installation of equipment and pipeline, and make steam or product pass in and out from the tube bank through same end head, can be favorable to prolonging flow path, guarantee in mixing chamber 13 with the heat transfer effect of raw materials.
Heating tube bank 111 and heat exchange tube bank 121 among steam evaporator 11 and product heat exchanger 12 in this embodiment are U type tube bank, and through the form of U type tube bank, do benefit to flowing medium and go out on single-ended head on the one hand, on the other hand still can reduce the leakage risk of material in hybrid chamber 13, make heating medium and raw materials medium effectively keep apart to avoid causing the influence to the methylamine synthesis reaction.
In the heating process of the mixing chamber 13, liquid raw materials such as methanol, liquid ammonia and recycled materials are very easy to cause entrainment of bubbles to the evaporated gas due to boiling of the liquid due to low boiling point, and particularly for the recycled materials, bubbles generated by boiling of the recycled materials may even have other solid impurities.
From this point of view, the horizontal housing 10 further comprises an evaporation chamber 14 located at the top of the mixing chamber 13, the evaporation chamber 14 communicating with the mixing chamber 13. A demister 141 for defoaming the evaporation gas raw material is installed in the evaporation chamber 14. The pressure of the evaporation gas can be effectively buffered in the evaporation chamber 14, different raw material gases can be preliminarily mixed in the evaporation chamber 14, the cleanliness of the evaporation gas can be ensured through the demister 141, and the blockage of a catalyst bed layer in the methylamine reactor 2 during reaction is avoided.
Through the evaporation mixer 1, the methylamine product after raw material synthesis can be effectively subjected to heat exchange in the product heat exchanger 12, and the liquid raw material in the evaporation mixer 1 is heated, so that a large amount of reaction heat generated in the synthesis reaction is recycled and comprehensively utilized, the whole reaction energy consumption is greatly reduced, and the production cost of unit product is effectively reduced.
Example 2
With reference to fig. 2, the present invention further provides a methylamine synthesis apparatus comprising the evaporation mixer 1, wherein the methylamine synthesis raw material in the evaporation mixer 1 is heated and evaporated, then heated and heated to further raise the temperature of the raw material, and then introduced into the methylamine reactor 2 for synthesis reaction.
A plurality of sections of catalytic units 20 distributed at intervals are arranged in the methylamine synthesizer, and each section of catalytic unit 20 comprises an equilibrium type catalyst layer 21 positioned at the upper part and a molecular sieve catalyst layer 22 positioned at the lower part.
The existing gas-phase catalytic reaction of methanol and ammonia is mainly used for producing dimethylamine raw material which is required by the market in large quantity and is suitable for producing DMF (dimethyl formamide), but the method has low yield of the dimethylamine and has higher energy consumption and material consumption for reaching the target capacity.
In the synthesis method, the gas phase catalytic reaction of methanol and ammonia is an exothermic reaction, and the reaction can be carried out at 360-425 ℃ in the presence of a catalyst.
In addition to the reaction of methanol with ammonia to form monomethylamine, dimethylamine and trimethylamine, the following reactions are carried out in the methylamine reactor 2:
CH3OH+CH3NH2→(CH3)2NH+H2O+Q
(CH3)3N+NH3→2(CH3)2NH-Q
2CH3NH2→(CH3)2NH+NH3+Q
2(CH3)2NH→CH3NH2+(CH3)3NH+Q
in actual production, the synthesis is performed by using an equilibrium catalyst for the different reactions, the product distribution is a thermodynamic equilibrium value, and when the ratio of ammonia to methanol is 2:1, the molar composition of monomethylamine, dimethylamine and trimethylamine is 22: 27: 51, the proportion of trimethylamine in the product is close to half, and although the yield of dimethylamine can be improved to some extent by increasing the reaction temperature, increasing the proportion of ammonia and methanol in the feed, and further reacting the trimethylamine feed back, a rectification separation system is usually required to enhance the separation, and the energy consumption and the material consumption of the system are undoubtedly increased.
By arranging the equilibrium catalyst layer 21 and the molecular sieve catalyst layer 22 in the methylamine reactor 2, dimethylamine can reach equilibrium concentration under the action of an equilibrium catalyst, and then trimethylamine adsorbed by the molecular sieve catalyst layer 22 continuously reacts with ammonia, and the dimethylamine and monomethylamine continuously move to a lower layer after passing through the molecular sieve catalyst layer 22 to reach an unbalanced state, so that the trimethylamine and ammonia further react to generate dimethylamine by converting the equilibrium reaction state into the unbalanced reaction state, and the aim of improving the conversion rate of the dimethylamine is fulfilled. The final dimethylamine formation is much higher than the equilibrium concentration and is a desired result for industrial production.
In this example, the equilibrium catalyst had a composition of SiO in terms of mass fraction225 parts of Al2O375 parts of a mixture; the molecular sieve catalyst comprises the following components: SiO 2215 parts of Al2O350 parts of aluminosilicate and 45 parts of aluminosilicate; the volume ratio of the equilibrium catalyst to the molecular sieve catalyst is 2.5: 1.
through detection, the yields of monomethylamine, dimethylamine and trimethylamine in the mixed methylamine product are respectively as follows: 22%, 45% and 33%.
Specifically, the volume ratio of the equilibrium catalyst to the molecular sieve catalyst is: (2-3): 1.
through the composition of the catalyst and the proportion of the two different catalysts, the selectivity of dimethylamine can be greatly improved, and the amount of the dimethylamine in the finally generated mixed methylamine is greatly improved.
The methylamine synthesizing device in the embodiment further comprises a reheating unit for reheating the raw materials evaporated in the evaporation mixer 1 so as to heat the reaction raw material gas and then introduce the heated reaction raw material gas into the methylamine reactor 2.
The reheating unit comprises a steam heater 5, a raw material preheater 6 and an electric heater 7 which are sequentially connected through pipelines, wherein a feed inlet of the steam heater 5 is connected with a discharge outlet of the evaporation mixer 1, and a discharge outlet of the electric heater 7 is connected with a feed inlet of the methylamine reactor 2. The reheating unit is used for further heating the evaporated and gasified gas raw materials to reach the temperature required by the reaction and then be introduced into the methylamine reactor 2, and the reheating unit can gradually increase the temperature of the gasified gas to ensure the normal operation of the gas raw materials in the methylamine reactor 2.
Specifically, the evaporated and mixed gas raw material firstly enters the tube side of a steam heater 5, the gas raw material in the tube side is heated by steam in the shell side of the steam heater 5 and then enters the tube side of a raw material preheater 6, and then enters an electric heater to finally reach the temperature required by the reaction and then enters a methylamine reactor 2.
It should be noted that the methylamine product generated in the methylamine reactor 2 is primarily cooled and heat exchanged by the raw material preheater 6 and then enters the product heat exchanger 12 in the evaporation mixer 1. The raw material preheater 6 is used as a heat exchanger for preheating the raw material gas, and also used for further exchanging heat and raising the temperature of the gas raw material heated by the steam heater 5 through the reaction heat carried by the methylamine product.
The raw material preheater 6 specifically comprises a shell side inlet and a shell side outlet, the shell side inlet is connected with a discharge port of the methylamine reactor 2, and the shell side outlet is connected with a feed port of the product heat exchanger 12. Through this kind of mode of setting, can make the methylamine product let in raw materials pre-heater 6's casing to carry out the heat transfer to the gaseous raw materials in the 6 tube passes of raw materials pre-heater, thereby further improved the rate of recovery of reaction heat, guaranteed gaseous raw materials's intensification effect simultaneously.
In order to ensure the normal supply of reaction raw materials, a circulation material tank 3 and a methanol raw material tank 4 are arranged at the upstream of the evaporation mixer 1, a circulation material feeding pump 31 and a methanol feeding pump 41 are respectively arranged at the bottoms of the circulation material tank 3 and the methanol raw material tank 4, and the circulation material and the methanol are respectively introduced into a mixing chamber 13 in the evaporation mixer 1 through the circulation material feeding pump 31 and the methanol feeding pump 41.
Based on the conversion of trimethylamine into dimethylamine in the methylamine reactor 2 and the supply amount required to avoid vaporizing ammonia in the mixer 1 to avoid a normal reaction. The methylamine synthesis device in the embodiment further comprises an ammonia gas feeding pipe, wherein ammonia gas feeding holes are formed in the evaporation mixer 1 and the methylamine reactor 2 respectively, and ammonia gas is introduced into the evaporation mixer 1 and the methylamine reactor 2 through the ammonia gas feeding holes respectively. Through the ammonia inlet pipe that sets up, can guarantee the excess state of ammonia raw materials and in methylamine reactor 2 to do benefit to the synthesis that promotes methylamine, guarantee the reaction effect.
The methylamine synthesis device can effectively reduce the energy consumption of the whole reaction process, reduce the separation load by improving the conversion rate of dimethylamine, and provide necessary conditions for energy conservation and consumption reduction of a downstream rectification separation system.
The devices of the methylamine synthesis device are connected through pipelines, specifically, a raw material circulating material pipeline is connected with a circulating material tank 3, the circulating material tank 3 is connected with a circulating material pump through a pipeline, and the circulating material pump is connected with an evaporation mixer 1 through a pipeline.
Raw materials methyl alcohol pipeline and methyl alcohol head tank 4 are connected, and methyl alcohol head tank 4 passes through the pipe connection with methyl alcohol raw material pump, and methyl alcohol raw material pump passes through the pipe connection with evaporation mixer 1.
Evaporation mixer 1 passes through the pipeline and is connected with steam heater 5, steam heater 5 passes through the pipeline and is connected with raw materials pre-heater 6, the import of 6 shell sides of raw materials pre-heater passes through the pipeline and is connected with 2 discharge gates of methylamine reactor, the shell side export of raw materials pre-heater 6 is connected with the product heat exchanger 12 of evaporation mixer 1, through letting in the shell side of raw materials pre-heater 6 with the methylamine product, can effectively heat the gas raw materials in the 6 tube side of raw materials pre-heater, the reaction heat that carries the methylamine product is retrieved tentatively.
Through being connected the shell side export of raw materials pre-heater 6 with the product heat exchanger 12 of evaporation mixer 1, can make the methylamine product let in the heat exchanger tube bank 121 of product heat exchanger 12 after preliminary heat transfer to heat the liquid raw materials in the mixing chamber 13 of evaporation mixer 1.
The heat exchange tube bundle 121 at the bottom of the evaporation mixer 1 is connected with a pipeline to a downstream separation system, and the mixed methylamine product is further separated.
The raw material liquid ammonia and the raw material gas ammonia are respectively connected with the evaporation mixer 1 through pipelines, and the heating tube bundle 111 of the steam evaporator 11 is respectively connected with an external steam supply pipeline and a steam condensate pipeline for leading out steam condensate.
The methylamine reactor 2 is composed of a vertical tower or a vertical container and internal parts, wherein the internal parts comprise three gas distributors and catalyst supporting pieces, and the three gas distributors are respectively arranged at the upper part of each section of catalytic unit 20. The catalyst support members include three, which support the three-stage catalytic units 20, respectively.
Each catalyst support is provided with two layers of catalysts, including an arrangement of equilibrium type methylamine reaction catalysts and molecular sieve catalysts, and three sections of six layers of catalysts at intervals are arranged in the methylamine reactor 2.
The methylamine synthesis device mainly comprises the following steps in work:
1) the mixed monomethylamine, trimethylamine, recombinant components and the like stored in the circulating material tank 3 are pressurized by a circulating material pump and are sent into the evaporation mixer 1 through a pipeline;
2) pressurizing the methanol stored in the liquid methanol tank by a methanol raw material pump to send the methanol into an evaporation mixer 1;
3) liquid ammonia is sent into the evaporation mixer 1 through a pipeline, and gas ammonia liquid ammonia is sent into the evaporation mixer 1 through a pipeline;
4) the liquid methanol, the liquid circulating material and the liquid ammonia are mixed and evaporated in the evaporation mixer 1, and simultaneously, the gas ammonia is also sent into the evaporation mixer 1 through a pipeline;
5) the heat source of the evaporation mixer 1 comprises two types, one type is high-temperature gas at the outlet of the methylamine reactor 2 after primary heat exchange by the raw material preheater 6, and the other type is externally supplied high-temperature steam.
6) The gaseous mixture after the evaporation of the misce bene in the evaporation mixer 1 at first passes through steam heater 5 preliminary heating up, then sends into the high temperature product gas heat transfer once more of raw materials pre-heater 6 and the export of methylamine reactor 2 through the pipeline, gets into electric heater 7 through the pipeline and heats to 360 ℃ and get into methylamine reactor 2, carries out abundant reaction at methylamine reactor 2 and generates mixed methylamine gas.
7) The temperature of the generated mixed methylamine gas is about 425 ℃, the mixed methylamine gas enters the raw material preheater 6 through a pipeline to preheat the raw material, the mixed methylamine gas coming out of the raw material preheater 6 enters the heat exchange tube bundle 121 of the product heat exchanger 12 of the evaporation mixer 1 to heat and evaporate the material, and the mixed methylamine gas coming out of the heat exchange tube bundle 121 is sent to downstream rectification and separation.
8) The externally supplied high-temperature steam is sent into a heating tube bundle 111 of the evaporation mixer 1 through a pipeline to heat and evaporate the material, and the steam condensate is sent out of the methylamine synthesis device through a pipeline.
In one particular example of this, the first and second,
feeding the circulating material at about 40 ℃ into a circulating material tank, and feeding the circulating material into an evaporation mixer through a circulating material pump; feeding raw material methanol with the temperature of about 25 ℃ into a methanol raw material tank, and feeding the raw material methanol into an evaporation mixer through a pipeline by a methanol raw material pump; liquid ammonia is sent into the evaporation mixer through a pipeline, and the three materials are mixed and evaporated in the evaporation mixer.
The mixed gas of evaporation gets into steam heater through the pipeline after the demister removes the foam, and the mixed gas preheats to about 170 ℃, and the mixed gas reentrants raw materials pre-heater carries out the heat transfer with methylamine reactor export gas, and the mixed gas preheats to about 360 ℃, gets into electric heater, and normal condition electric heating is out of work, and the heat is supplemented with the electric heating when not enough. The method comprises the following steps of enabling a mixed gas at 360 ℃ to enter a methylamine reactor, enabling all substances in the methylamine reactor to generate a chemical reaction to generate a mixed methylamine gas, enabling the reaction to be an exothermic reaction, enabling the temperature of the mixed methylamine gas after the reaction to reach about 430 ℃, enabling the high-temperature methylamine mixed gas at the outlet of the methylamine reactor to enter a raw material preheater to exchange heat with the evaporated mixed gas to reach about 200 ℃, enabling the high-temperature methylamine mixed gas to enter a heat exchange tube bundle at the bottom of an evaporation mixer to be used for evaporating raw materials, enabling the mixed methylamine coming out of the heat exchange tube bundle to have a temperature of about 140 ℃, and enabling the mixed methylamine gas to enter a downstream rectification separation process.
The steam enters a heating tube bundle at the bottom of the evaporation mixer through a pipeline and exchanges heat with the raw material to supplement the heat of evaporation.
In current raw materials evaporation mixing process, mainly including vertical evaporation mixing tank to and set up two reboilers in evaporation mixing tank bottom, through letting in steam to two reboilers, heat the evaporation to the raw materials that lets in the evaporation mixing tank, through current evaporation mixing arrangement, the steam consumption volume of producing 1t mixed methylamine is 8.1 t.
The raw materials are heated and evaporated by the evaporation mixer in the example of the invention, the steam consumption for producing 1t of mixed methylamine is 6.5t, and the comparison shows that 1.6t of steam can be saved by introducing the methylamine product into the heat exchange tube bundle of the product heat exchanger in the evaporation mixer, the dimethylamine content of the mixed methylamine can reach about 45%, and the energy consumption of the subsequent rectification is greatly reduced.
The following examples are given for the catalyst ratios of the present invention, and the different examples are all carried out under the reaction conditions given in the above examples.
Example 3
In this example, the equilibrium catalyst had a composition of SiO in terms of mass fraction230 parts of Al2O370 parts of (B); the molecular sieve catalyst comprises the following components: SiO 2220 parts of Al2O360 parts of aluminosilicate and 50 parts of aluminosilicate; the volume ratio of the equilibrium catalyst to the molecular sieve catalyst is 3: 1.
the yields of monomethylamine, dimethylamine and trimethylamine in the mixed methylamine product are respectively as follows: 20%, 42% and 38%.
Example 4
In this example, the equilibrium catalyst comprises the following components in mass fraction: SiO 2215 parts of Al2O385 parts of a mixture; the molecular sieve catalyst comprises the following components: SiO 2210 parts of Al2O340 parts of aluminosilicate and 50 parts of aluminosilicate; the volume ratio of the equilibrium catalyst to the molecular sieve catalyst is 2: 1.
the yields of monomethylamine, dimethylamine and trimethylamine in the mixed methylamine product are respectively as follows: 18%, 40% and 42%.
Example 5
In the embodiment, only the equilibrium type catalyst is included, and the component of the equilibrium type catalyst is SiO225 parts of Al2O3And 75 parts.
The yields of monomethylamine, dimethylamine and trimethylamine in the mixed methylamine product are respectively as follows: 22%, 27% and 51%.
Example 6
The equilibrium catalyst and molecular sieve catalyst components in this example were essentially the same as in example 3, except that the volume ratio of equilibrium catalyst to molecular sieve catalyst was 4: 1.
the yields of monomethylamine, dimethylamine and trimethylamine in the mixed methylamine product are respectively as follows: 23%, 28% and 49%.
Example 7
The components of the equilibrium catalyst and the molecular sieve catalyst in this example were the same as in example 2, except that the volume ratio of the equilibrium catalyst to the molecular sieve catalyst was 1: 1.
the yields of monomethylamine, dimethylamine and trimethylamine in the mixed methylamine product are respectively as follows: 22%, 30% and 48%.
It can be seen from different examples that the ratio of the equilibrium catalyst to the molecular sieve catalyst in the invention is an important factor influencing the yield of dimethylamine in the mixed methylamine, and the more the equilibrium catalyst is, the more trimethylamine is generated, so that the amount of trimethylamine in the mixed methylamine is at a higher level.
After the molecular sieve catalyst is added, the molecular sieve catalyst plays a role in adsorbing a trimethylamine product, so that part of the trimethylamine can be continuously converted, but when the amount of the balanced catalyst is excessively larger than that of the molecular sieve catalyst, the yield of the dimethylamine can not be obviously improved.
By controlling the amount between the equilibrium catalyst and the molecular sieve catalyst to be (2-3) in the present invention: 1 range, can effectively balance the reaction of various methylamine products with methanol or ammonia gas, and obviously improve the selectivity of dimethylamine, thereby being beneficial to the reaction towards an industrial ideal direction.
It is important to point out that the methylamine product in the methylamine reactor is introduced into the raw material preheater and the heat exchange tube bundle in the evaporation mixer, so that the reaction heat of the synthesis reaction can be recycled to the maximum extent, thereby being beneficial to reducing the energy consumption of the methylamine unit product, improving the conversion rate of dimethylamine by combining the molecular sieve catalyst, reducing the energy consumption and the power consumption of downstream rectification separation, and greatly improving the product competitiveness.
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 (8)

1. An evaporative mixer, comprising: the horizontal shell is provided with a horizontal shell,
a steam evaporator and a product heat exchanger are oppositely arranged in the horizontal shell;
the steam evaporator comprises a heating tube bundle and a steam feeding and discharging end socket, and the product heat exchanger comprises a heat exchange tube bundle and a product feeding and discharging end socket;
the methylamine product enters the horizontal shell to recover the heat of the methylamine product;
the horizontal shell comprises a mixing chamber for mixing and heating raw materials, and the heating tube bundle and the heat exchange tube bundle are both arranged in the mixing chamber;
the horizontal shell also comprises an evaporation chamber positioned at the top of the mixing chamber, and the evaporation chamber is communicated with the mixing chamber;
the pressure of the evaporation gas can be effectively buffered in the evaporation chamber, and different raw material gases can be preliminarily mixed in the evaporation chamber;
the upper reaches of evaporation mixer are provided with circulation material jar and methyl alcohol head tank, and circulation material and methyl alcohol are let in respectively through circulation material feed pump and methyl alcohol feed pump the mixing chamber.
2. The evaporative mixer of claim 1, wherein the vapor feed and discharge head and the product feed and discharge head are each one and are disposed at each end of the horizontal housing.
3. The evaporative mixer of claim 1, wherein the heating tube bundle and the heat exchange tube bundle are U-shaped tube bundles.
4. The evaporative mixer of claim 3, wherein a demister for defoaming the evaporative gas is installed in the evaporation chamber.
5. A methylamine synthesis device, which is characterized in that the device comprises the evaporation mixer of any one of claims 1-4, the methylamine synthesis raw material in the evaporation mixer is reheated and then enters a methylamine reactor for synthesis reaction, a plurality of sections of catalytic units are arranged in the methylamine reactor, each section of catalytic unit comprises a balanced catalyst layer at the upper part and a molecular sieve catalyst layer at the lower part;
the components of the equilibrium catalyst are respectively as follows by mass fraction: SiO 2215 to 30 parts of Al2O370-85 parts of a solvent; the molecular sieve catalyst comprises the following components in percentage by mass: SiO 2210 to 20 parts of Al2O340-60 parts of aluminosilicate and 40-50 parts of aluminosilicate;
the volume ratio of the equilibrium catalyst to the molecular sieve catalyst is as follows: (2-3): 1.
6. the methylamine synthesis apparatus according to claim 5, further comprising a reheating unit for reheating, wherein the reheating unit comprises a steam heater, a raw material preheater and an electric heater which are arranged in sequence, a feed inlet of the steam heater is connected with a discharge outlet of the evaporation mixer, and a discharge outlet of the electric heater is connected with a feed inlet of the methylamine reactor.
7. The methylamine synthesis apparatus of claim 6, wherein the feedstock preheater comprises a shell-side inlet and a shell-side outlet, the shell-side inlet being connected to the outlet of the methylamine reactor, and the shell-side outlet being connected to the inlet of the product heat exchanger.
8. The methylamine synthesis apparatus according to claim 5, further comprising an ammonia gas inlet pipe, wherein the evaporation mixer and the methylamine reactor are respectively provided with an ammonia gas inlet, and ammonia gas is introduced into the evaporation mixer and the methylamine reactor through the ammonia gas inlet.
CN202111000732.7A 2021-08-30 2021-08-30 Evaporation mixer and methylamine synthesis device Active CN113813879B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202111000732.7A CN113813879B (en) 2021-08-30 2021-08-30 Evaporation mixer and methylamine synthesis device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202111000732.7A CN113813879B (en) 2021-08-30 2021-08-30 Evaporation mixer and methylamine synthesis device

Publications (2)

Publication Number Publication Date
CN113813879A CN113813879A (en) 2021-12-21
CN113813879B true CN113813879B (en) 2022-05-27

Family

ID=78923480

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202111000732.7A Active CN113813879B (en) 2021-08-30 2021-08-30 Evaporation mixer and methylamine synthesis device

Country Status (1)

Country Link
CN (1) CN113813879B (en)

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN204676015U (en) * 2015-04-22 2015-09-30 江苏金凯树脂化工有限公司 A kind of dimethylamine retrieving arrangement

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE875674A (en) * 1978-04-21 1979-10-18 Ici Ltd AMINE PRODUCTION
JPS59210050A (en) * 1983-05-13 1984-11-28 Nitto Chem Ind Co Ltd Production of dimethylamine
US7115238B2 (en) * 2002-05-24 2006-10-03 Mitsubishi Gas Chemical Company, Inc. Crystalline silicoaluminophosphate salt molecular sieve having octaoxygen-membered ring pore, process for producing the same and process for producing methylamine with the molecular sieve as catalyst
CN203459056U (en) * 2013-09-23 2014-03-05 山东华鲁恒升化工股份有限公司 Methylamine synthesizer
CN110918022A (en) * 2019-11-29 2020-03-27 安阳九天精细化工有限责任公司 Temperature regulating system in methylamine synthesis

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN204676015U (en) * 2015-04-22 2015-09-30 江苏金凯树脂化工有限公司 A kind of dimethylamine retrieving arrangement

Also Published As

Publication number Publication date
CN113813879A (en) 2021-12-21

Similar Documents

Publication Publication Date Title
US4865624A (en) Method for steam reforming methanol and a system therefor
CN112142004B (en) Hydrogen production and purification method by methanol-water reforming reaction
CN102766021B (en) Production system and production method for continuously producing ethanol by ethyl acetate through using hydrogenation
CN110218151B (en) Device and method for preparing propyl propionate through tower kettle flash evaporation type heat pump reaction rectification
CN103240036B (en) A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application
US4376758A (en) Process for synthesizing ammonia from hydrocarbons
CN114634160B (en) Full-flow method and device for thermochemical zinc-sulfur-iodine cycle coupling methane hydrogen production
CN113461027A (en) Low-pressure synthetic ammonia tower and renewable energy source low-pressure synthetic ammonia system
CN104826557A (en) Synthesis reactor using self reaction heat to heat feed medium
CN116078313B (en) Continuous bromoethane preparation system and preparation process
CN113813879B (en) Evaporation mixer and methylamine synthesis device
CN215996580U (en) Evaporation mixer and methylamine synthesis device
CN1100412A (en) Stripping recirculation technology & apparatus for urea production
CN102502697B (en) Method for recovering ammonia in morpholine solution
CN113856607B (en) DMAC (dimethyl acetamide) reaction device for thermal condensation of dimethylamine and acetic acid and application method thereof
CN102391082B (en) Method and device for heat exchange of methanol in production of formaldehyde
CN109133003A (en) Methanol hydrogen production system for integrated fuel cell of pure electric vehicle
CN212594064U (en) Durene rectification separator
CN211283719U (en) Novel thermodynamic system for thermal power coupling methanol hydrogen production
CN114618392A (en) Reaction system and method for preparing hydrocyanic acid
CN114907186A (en) Method for directly preparing methanol from carbon dioxide and hydrogen
CN210796289U (en) High-efficient low energy consumption sodium methoxide purification equipment
CN207210294U (en) A kind of process units of energy-saving acetic acid hydrogenation or ethyl acetate preparation of ethanol by hydrogenating
CN209081426U (en) Methanol hydrogen production system for integrated fuel cell of pure electric vehicle
CN113636925B (en) System and method for preparing high-concentration formaldehyde from methylal

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant