CN109369607A - A kind of device and method of azeotropic catalysis reaction synthesizing triformol - Google Patents
A kind of device and method of azeotropic catalysis reaction synthesizing triformol Download PDFInfo
- Publication number
- CN109369607A CN109369607A CN201811358845.2A CN201811358845A CN109369607A CN 109369607 A CN109369607 A CN 109369607A CN 201811358845 A CN201811358845 A CN 201811358845A CN 109369607 A CN109369607 A CN 109369607A
- Authority
- CN
- China
- Prior art keywords
- azeotropic
- tower
- catalytic
- section
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D323/00—Heterocyclic compounds containing more than two oxygen atoms as the only ring hetero atoms
- C07D323/04—Six-membered rings
- C07D323/06—Trioxane
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention discloses the device and method that a kind of azeotropic is catalyzed reaction synthesizing triformol, including feed pump, heater, azeotropic catalytic tower, the finished product rectifying column being sequentially connected, raw material formalin and dehydrating agent are first into heating in the tube side of heater, then into being dehydrated in azeotropic catalytic tower, the result of dehydration is divided into two-phase: gas phase ascends into evaporator section and flows out outside tower, and liquid phase falls under gravity into catalytic section and carries out polymerization reaction；Polymerizate is imported into rectifying column, obtains product metaformaldehyde finished product after being fractionated.After formalin is mixed with dehydrating agent, under the synergistic effect that azeotropic dehydration, concentrate are catalyzed, produce high-purity metaformaldehyde product, it overcomes existing water absorption techniques, concentration technique, sulfuric acid catalysis technology, extract defect and drawback existing for drying technology, having started one, process conditions are mild, process is short, investment is small, new technology both with quick, efficient low-consume, clean and environmental protection many advantages.
Description
Technical field
The present invention relates to a kind of synthesizer of metaformaldehyde and methods, and in particular to a kind of azeotropic catalysis reaction synthesis three
The device and method of polyformaldehyde, belong to technical field of fine.
Background technique
Metaformaldehyde is important industrial chemicals, very widely used.At present in technique comparative maturity synthetic technology road
Line is: using the formalin of 35-45% as raw material, using fluid sulphuric acid as catalyst synthesizing triformol, thus to synthesis
The process bands of metaformaldehyde carry out inadequate natural endowment: three waste discharge is more, production environment is poor, long flow path, investment is big, production equipment corrosion is tight
The problems such as weight, therefore it is imperative to develop a kind of energy-efficient, clean and environmental protection new technology.
Existing synthetic method are as follows: the formalin of 35-45% content → 100 DEG C of reduced pressure → heating → entrance is warded off
Porcelain reaction kettle → obtained finally with the extracting and refining → drying of 2-10% sulfuric acid catalysis → evaporation and concentration metaformaldehyde aqueous solution → again
Finished product.And this technology is that tubulation bed reactor is catalyzed with azeotropic, directly integrates azeotropic dehydration, catalysis with formalin,
And under the action of dehydrating agent, while dehydration, catalyzing cooperation effect occurs, together a kind of new technology of synthesizing triformol.
Summary of the invention
The technical problem to be solved by the present invention is to catalyze and synthesize existing for metaformaldehyde for sulfuric acid process in the prior art
Inadequate natural endowment, and a kind of device and method that azeotropic catalyzes and synthesizes metaformaldehyde are provided, overcome existing water absorption techniques, concentration
Technology, sulfuric acid catalysis technology, defect and drawback existing for extraction drying technology etc., have started that a process conditions are mild, technique
Process is short, investment is small, the method and device of quick, efficient low-consume, clean and environmental protection.
To achieve the goals above, the present invention adopts the following technical scheme:
A kind of device of azeotropic catalysis reaction synthesizing triformol, feed pump, heater, azeotropic including being sequentially connected are urged
Change reaction tower, finished product rectifying column, raw material formalin and dehydrating agent are first into heating in the tube side of heater, then into
Enter into azeotropic catalytic tower and be dehydrated, the result of dehydration is divided into two-phase: gas phase ascends into azeotropic dehydration section and flows out
Outside tower, liquid phase falls under gravity into catalytic section and carries out polymerization reaction；Polymerizate is imported into rectifying column, is fractionated
After obtain product metaformaldehyde finished product；It is characterized by:
The feed pump, be equipped with import 7A and outlet 7B, in which: import 7A and be capable of providing raw material formalin with
The device of dehydrating agent is connected；
The heater is equipped with import 6A and outlet 6B, in which: import 6A is connected with the outlet 7B of feed pump；
The azeotropic catalytic tower, top is equipped with gaseous phase outlet 1A, bottom is equipped with discharge port 1E, and the top of side wall is set
There are the first reflux liquid inlet mouth 1B, middle part to be equipped with feed inlet 1C, middle and lower part is equipped with heating liquid outlet 1F and heating liquid import 1D, lower part
Equipped with the second reflux liquid inlet mouth 1G, the position for heating liquid import 1D exports 1F lower than heating liquid；Wherein: feed inlet 1C and heater
Outlet 6B be connected；Gaseous phase outlet 1A is connected with condenser I, return tank I and reflux pump I in turn, the pump discharge of reflux pump I with
First reflux liquid inlet mouth 1B is connected；Heating liquid import 1D is connected with heat-exchanger pump, heating liquid outlet 1F and hot-water collection system
It is connected；
The finished product rectifying column, top is equipped with gaseous phase outlet 8C, bottom is equipped with finished product discharge port 8D, is equipped with above side wall
Refluxing opening 8B, middle part are equipped with feed inlet 8A, in which: feed inlet 8A is connected with the discharge port 1E of azeotropic catalytic tower；Gas phase
Outlet 8C is connected with condenser II, return tank II and reflux pump II in turn；The pump discharge of reflux pump is divided into three tunnels, all the way with reflux
Mouthful 8B is connected, and another way is connected with the first reflux liquid inlet mouth 1B of azeotropic catalytic tower, and the of third road and azeotropic catalytic tower
Two 1G mouthfuls of reflux liquid inlet mouths are connected, and continue into azeotropic catalytic tower and are persistently dehydrated and recycle；Discharge port 8D with adopt
The device for collecting or receiving finished product metaformaldehyde is connected.
In above-mentioned technical proposal, the azeotropic catalytic tower, interior top is equipped with demister, packet below the demister
The catalytic section of superposed azeotropic dehydration section and lower part is included, the top of the azeotropic dehydration section sets gradually distribution from top to bottom
Device, flase floor；The top of the catalytic section sets gradually distributor, flase floor from top to bottom, and the bottom of the catalytic section is from upper
Distributor, bed course, flase floor are successively arranged under；The azeotropic dehydration section be equipped with tower internals, the tower internals be include regular
Any one in filler or column plate；It includes structured packing that the tower internals, which is selected, and the structured packing loads number of segment as N, and 1
≤ N≤100, every section of height are that distributor, flase floor are equipped between 1-3 meters, each section, the distributor the flase floor it
On；Or it includes column plate that the tower internals, which is selected, the number of plates is M, 1≤M≤100；The catalytic section includes tubulation bed, institute
The number of segment for stating catalytic section is N, and 1≤N≤10 are successively arranged distributor, bed course, flase floor between each section from top to bottom；
The tubulation bed includes the more tubulations being vertically arranged, and fills module catalyst in the tubulation, the tubulation outer wall and
It reacts to heat liquid stream road between inner wall of tower, closed guard will be respectively provided at the top and bottom of the tubulation bed to be added on fluid conduit
Lower end closure, the baffle are equipped with the corresponding tubulation two open ends of multiple open communications；The azeotropic dehydration section flows down anti-
Raw material is answered to sequentially pass through each distributor in catalytic section described in multistage, bed course, flase floor, tubulation discharge；
Gaseous phase outlet 1A, bottom are equipped at the top of the azeotropic catalytic tower equipped with discharge port 1E, the azeotropic catalysis is anti-
It answers and is urged positioned at tubulation bed bottom setting heating liquid import 1D, the heating liquid opposite side import 1D in the azeotropic on tower side wall
Change the upper setting heating liquid at the top of tubulation bed of reaction tower side wall and exports 1F, the distributor of the azeotropic catalytic tower topmost
The distributor for being connected to the first reflux liquid inlet mouth 1B, lowest part that are arranged on its side wall is connected to second be arranged on its side wall and flows back into
Liquid mouth 1G, the distributor above the tower internals at middle part are connected to the feed inlet being arranged on the azeotropic catalytic tower side wall
1C。
In above-mentioned technical proposal, five shape knots layer by layer that the bed course is quartz sand or porcelain ball to be combined into variable grain degree
Structure, five laminate is Pyatyi gradation: i.e. top layer's granularity close to or slightly larger than the catalyst particle
Degree, undermost granularity be slightly larger than the flase floor gap dimension, between three layers from top to bottom, by small gradually big, upper and lower grain
Degree linking arrangement, every thickness degree is in 5~15cm.
In above-mentioned technical proposal, the demister, distributor, flase floor, material are all stainless steels.
In above-mentioned technical proposal, heating liquid import 1D and heating liquid outlet 1F are equipped in each section of catalytic section.
In above-mentioned technical proposal, the module catalyst, structure is with the module catalyst in patent 201620189729.2:
Including catalyst, wire mesh, wire mesh corrugated plating, the module catalyst is by the wire mesh, wire mesh wave
Card spaced and parallel setting installs the catalyst granules between wire mesh described in two panels and forms catalyst layer, and this is urged
The catalyst granules in agent layer by the wire mesh corrugated plating apart from；Institute in the module catalyst
State the setting of catalyst layer interval.
In above-mentioned technical proposal, the catalyst in the module catalyst is highly acidic resin catalyst, high temperature resistant strong acid
The superpower acid resin catalyst of resin catalyst, carried metal；It is preferred that spherical or pearl highly acidic resin catalyst, high temperature resistant
The superpower acid resin catalyst of strong acid resin catalyst or carried metal；The type of carried metal is the main group II of the periodic table of elements
With VIII group element, load capacity is the 1-20% of resin catalyst exchange capacity.
In above-mentioned technical proposal, every section of tubulation pipe number is F, 1≤F≤10x104；Every root canal diameter is E, 2≤E≤30cm.
In above-mentioned technical proposal, the azeotropic catalytic tower, being added to the dehydrating agent in it from feed pump is dichloro
Ethane, benzene, aromatic hydrocarbons, any one or two kinds or more the mixtures being mixed in any proportion in hexamethylene.
In above-mentioned technical proposal, the return tank I is equipped with inlet, leakage fluid dram and discharge outlet, and inside is equipped with coalescence
Device；Wherein, inlet is connected with the outlet of condenser I, and leakage fluid dram is mutually connected with the pump inlet of reflux pump I, discharge outlet with
Waste water treatment system is connected, and gas phase forms liquid phase after condenser I condensation, into after in return tank I, in coalescer and static state
The water taken off is discharged by discharge outlet under the double action of layering.
In above-mentioned technical proposal, the finished product rectifying column, side wall lower section is installed on reboiler.
In the present invention, the condenser I, return tank I, coalescer, reflux pump I, heater, feed pump, finished product rectifying
Tower, reboiler, condenser II, return tank II, reflux pump II are this field commercial product, or the routine with corresponding function produces
Product.
The present invention also provides a kind of azeotropic be catalyzed reaction synthesizing triformol method, flow chart as shown in Figure 1, include with
Lower step:
(1) azeotropic dehydration: reach azeotropic temperature, water and part after formalin, dehydrating agent are heated to 50-100 DEG C
Dehydrating agent becomes gas phase to achieve the purpose that water export formaldehyde is concentrated, and the mixture formed after dehydration is the formalin of concentration
Solution and a small amount of unvaporized dehydrating agent；And the water of gas phase and partially dehydrated dose formed after being condensed, being coalesced liquid phase water and
The dehydrating agent of liquid phase, the water discharge of liquid phase, the dehydrating agent of liquid phase recycle；
(2) polymerization reaction: the mixture formed in step (1), the formalin of concentration therein, catalyst A's
Polymerization reaction is carried out under catalytic action and generates metaformaldehyde aqueous solution, and after polymerization reaction, product is metaformaldehyde aqueous solution
With a small amount of unvaporized dehydrating agent；
(3) finished product is fractionated: the product formed in step (2) is fractionated in a heated state, obtains gas phase and liquid phase；
Gas phase is dehydrating agent and a small amount of water present in product, is back in step (1) and follows through the reflux of condensation rear portion, a part
Ring utilizes, and liquid phase is product metaformaldehyde finished product, harvesting.
In above-mentioned technical proposal, method specifically includes the following steps:
(1) azeotropic dehydration: formalin, dehydrating agent are imported into the tube side of heater by feed pump and are heated,
Reach azeotropic temperature after being heated to 50-100 DEG C under the conditions of normal pressure or micro-positive pressure, azeotropic catalytic tower is imported by feed inlet 1C
Azeotropic dehydration section in carry out azeotropic dehydration, achieve the purpose that formaldehyde is concentrated, under the action of azeotropic principles, form two in tower
Phase: gas phase is water and partially dehydrated dose, and liquid phase is the formalin and a small amount of unvaporized dehydrating agent after dehydration concentration；Its
In: gas phase rises to tower top and is discharged from gaseous phase outlet 1A, and the water and dehydrating agent of liquid phase, liquid phase are formed after condenser I condensation
Water and dehydrating agent the water taken off is discharged by discharge outlet under the double action of coalescer and static layering in return tank I,
The dehydrating agent of liquid phase is then refluxed pump I and is pumped to the first refluxing opening 1B to which infinite reflux recycles benefit into azeotropic catalytic tower
With；And it is dehydrated the formalin after concentration and a small amount of unvaporized dehydrating agent, azeotropic can be come downwards under gravity
In the catalytic section of catalytic tower；
(2) polymerization reaction: the formalin after dehydration concentration comes downwards in the tubulation bed of catalytic section, urging in tubulation
Polymerization reaction is carried out under the catalytic action of agent and generates metaformaldehyde aqueous solution, and after polymerization reaction, product is metaformaldehyde
Aqueous solution and a small amount of unvaporized dehydrating agent；Product is continued traveling downwardly under the effect of gravity to tower bottom, be discharged by discharge port 1E and
It is imported into finished product rectifying column by feed inlet 8A；The heating liquid import 1D of catalytic section is connected with heat-exchanger pump, what heat-exchanger pump provided
Hot water enters in the shell side of catalytic section, provides temperature, heating liquid outlet 1F and hot-water collection system for the polymerization reaction in tubulation
System is connected；
(3) finished product is fractionated: after the product formed in step (2) imported into finished product rectifying column, in the heated condition of reboiler
Under be fractionated, obtain gas phase and liquid phase；Gas phase is dehydrating agent and a small amount of water present in product, is discharged through gaseous phase outlet 8C
And enter in condenser II and condensed, the dehydrating agent and a small amount of water condensed is followed by return tank II, reflux pump
It is divided into three tunnels after II, is connected all the way with refluxing opening 8B, another way is connected with the first reflux liquid inlet mouth 1B of azeotropic catalytic tower,
Third road is connected with the second reflux liquid inlet mouth 1G that tubulation bed lowest part distributor is connected to, and continues into tubulation bed and continues
It is dehydrated and recycles；The pure metaformaldehyde product of the obtained liquid phase, that is, finished product of tower bottom is discharged collected by discharge port 8D.
In above-mentioned technical proposal, in step (1), the proportion of dehydrating agent and formalin is formed by azeotropic and concentration of formaldehyde
Depending on, 1-10:1 can be rested in mass ratio；The mass ratio of formaldehyde i.e. in dehydrating agent and formalin is 1-10:1；Formaldehyde
The mass fraction of formaldehyde in aqueous solution is 30-55%.
In above-mentioned technical proposal, in step (1), the dehydrating agent is purified petroleum benzin, in aromatic hydrocarbons, dichloroethanes, hexamethylene
Any one or two kinds or more the mixtures being mixed in any proportion.
In above-mentioned technical proposal, in step (2), the catalyst is highly acidic resin catalyst, high temperature resistant strong resin
The superpower acid resin catalyst of catalyst, carried metal；It is preferred that spherical or pearl highly acidic resin catalyst, high temperature resistant strong acid
The superpower acid resin catalyst of resin catalyst or carried metal；The type of carried metal be the periodic table of elements main group II and
VIII group element, load capacity are the 1-20% of resin catalyst exchange capacity.
In above-mentioned technical proposal, in step (2), the heat-exchanger pump, the temperature of the hot water provided is 80-120 DEG C, is guaranteed
The temperature of polymerization reaction is 70-110 DEG C in tubulation bed.
In above-mentioned technical proposal, in step (3), the finished product rectifying column, operating condition are as follows: tower top temperature: 30-110
℃；Column bottom temperature: 80-180 DEG C；Operating pressure: 0.01-1.5Mpa.
In above-mentioned technical proposal, in step (3), the dehydrating agent and a small amount of water condensed is back into from refluxing opening 8B
In product rectifying column, reflux ratio 0.1-2.0.
The advantages of technical solution of the present invention, is:, will be more instead of the connection of multiple distributing components in existing equipment
Kind function is integrated in a reaction tower, is enormously simplified production technology, is shortened the reaction time, and metaformaldehyde is efficiently being produced
When significant effect.After formalin is mixed with entrainer, under the synergistic effect that azeotropic dehydration, concentrate are catalyzed, produce high-purity
Metaformaldehyde product overcomes existing: water absorption techniques, concentration technique, sulfuric acid catalysis technology, extraction drying technology existing for lack
Fall into and drawback, started that a process conditions are mild, and process flow is short, invest it is small, it is quick；Efficient low-consume, clean and environmental protection are all
Novel technique route both with more advantages.
Detailed description of the invention
Fig. 1 are as follows: azeotropic catalyzes and synthesizes the flow chart of the method for metaformaldehyde in the present invention；
Fig. 2 are as follows: azeotropic catalyzes and synthesizes the structure chart of the device of metaformaldehyde in the present invention；
Fig. 3 are as follows: the schematic diagram of internal structure of azeotropic catalytic tower；
Fig. 4 are as follows: the structural schematic diagram of single tubulation cross-section module catalyst；
Wherein: 1- azeotropic catalytic tower, the first reflux liquid inlet mouth 1B, 103- feed inlet of 101- gaseous phase outlet 1A, 102-
1C, 104- heat liquid import 1D, 105- discharge port 1E, and 106- heats liquid and exports 1F, 107- the second reflux liquid inlet mouth 1G, 2- condensation
Device I, 3- return tank I, 4- coalescer, 5- reflux pump I, 6- heater, 7- feed pump, 8- finished product rectifying column, 9- reboiler, 10-
Condenser II, 11- return tank II, 12- reflux pump II；13- demister, 14- distributor, 15- tower internals, 16- tubulation bed, 17-
Tubulation, 18- bed course, 19- flase floor, 40- module catalyst, 401- catalyst layer, 402- wire mesh, 403- wire mesh wave
Card.
Specific embodiment
The specific embodiment of technical solution of the present invention is described in detail below, but the present invention is not limited in being described below
Hold:
Present invention firstly provides the devices that a kind of azeotropic is catalyzed reaction synthesizing triformol, including the feed pump being sequentially connected
7, heater 6, azeotropic catalytic tower 1, finished product rectifying column 8, raw material formalin and dehydrating agent are first into heater 6
Tube side in heating, then into being dehydrated in azeotropic catalytic tower, the result of dehydration is divided into two-phase: gas phase rise into
Enter azeotropic dehydration section and flow out outside tower, liquid phase falls under gravity into catalytic section and carries out polymerization reaction；Polymerizate is led
Enter into rectifying column 8, obtains product metaformaldehyde finished product after being fractionated；It is as in Figure 2-4:
The feed pump 7 is equipped with import 7A and outlet 7B, in which: import 7A and be capable of providing raw material formalin
It is connected with the device of dehydrating agent；
The heater 6 is equipped with import 6A and outlet 6B, in which: import 6A is connected with the outlet 7B of feed pump；
The azeotropic catalytic tower 1, top is equipped with gaseous phase outlet 1A 101, bottom is equipped with discharge port 1E 105, side
The top of wall is equipped with the first reflux liquid inlet mouth 1B 102, middle part is equipped with feed inlet 1C 103, middle and lower part is equipped with heating liquid and exports 1F
106 and heating liquid import 1D 104, lower part are equipped with the second reflux liquid inlet mouth 1G 107, and the position of heating liquid import 1D is lower than heating
Liquid exports 1F；Wherein: feed inlet 1C is connected with the outlet 6B of heater 6；Gaseous phase outlet 1A be connected in turn condenser I 2,
Return tank I 3 and reflux pump I 5, the pump discharge of reflux pump I are connected with the first reflux liquid inlet mouth 1B；Heat liquid import 1D and heat
Water pump is connected, and heating liquid outlet 1F is connected with hot-water collection system；
The finished product rectifying column 8, top is equipped with gaseous phase outlet 8C, bottom is equipped with finished product discharge port 8D, sets above side wall
There are refluxing opening 8B, middle part to be equipped with feed inlet 8A, in which: feed inlet 8A is connected with the discharge port 1E of azeotropic catalytic tower；Gas
Mutually outlet 8C is connected with condenser II 10, return tank II 11 and reflux pump II 12 in turn；The pump discharge of reflux pump 12 is divided into three
Road is connected with refluxing opening 8B all the way, and another way is connected with the first reflux liquid inlet mouth 1B of azeotropic catalytic tower, and third road is together
1G mouthfuls of the second reflux liquid inlet mouth of boiling catalytic tower is connected, and continues into azeotropic catalytic tower and is persistently dehydrated and recycles；
Discharge port 8D is connected with the device for acquiring or receiving finished product metaformaldehyde.
The azeotropic catalytic tower 1, interior top are equipped with demister 13, include being located at top below the demister 13
Azeotropic dehydration section and lower part catalytic section, the top of the azeotropic dehydration section sets gradually distributor 14, grid from top to bottom
Plate 19；The top of the catalytic section sets gradually distributor 14, flase floor 19 from top to bottom, the bottom of the catalytic section from up to
Under be successively arranged distributor 14, bed course 18, flase floor 19；The azeotropic dehydration section is equipped with tower internals 15, and the tower internals 15 is
Including any one in structured packing or column plate；It includes structured packing that the tower internals 15, which is selected, the structured packing filling
Number of segment is N, and 1≤N≤100, every section of height are to be equipped with distributor 14, flase floor 19, the distribution between 1-3 meters, each section
Device 14 is on the flase floor 19；Or it includes column plate that the tower internals 15, which is selected, the number of plates is M, 1≤M≤100；
The catalytic section includes tubulation bed 16, and the number of segment of the catalytic section is N, 1≤N≤10, is successively arranged from top to bottom between each section
Distributor 14, bed course 18, flase floor 19；
The tubulation bed 16 includes the more tubulations 17 being vertically arranged, and fills module catalyst 40, the column in the tubulation 17
It is heating liquid stream road between 1 inner wall of 17 outer wall of pipe and reaction tower, the top and bottom of the tubulation bed 16 are respectively provided with closed guard
Fluid conduit upper and lower side closure will be added, the baffle is equipped with corresponding 17 two open ends of tubulation of multiple open communications；It is described total
The reaction raw materials that boiling dewatering period flows down sequentially pass through each distributor 14, bed course 18, flase floor in catalytic section described in multistage
19, tubulation 17 is discharged；
Gaseous phase outlet 1A 101 is equipped at the top of the reaction tower 1, bottom is equipped with discharge port 1E 105,1 side of reaction tower
It is located at 16 bottom of tubulation bed setting heating liquid import 1D 104,104 opposite side heating liquid import 1D on wall described anti-
It answers and is located at setting heating liquid outlet 1F 106 at the top of tubulation bed 16 on 1 side wall of tower, the distributor 14 of 1 topmost of reaction tower connects
The distributor 14 for leading to the first reflux liquid inlet mouth 1B 102, lowest part that are arranged on its side wall is connected to second time be arranged on its side wall
Flow inlet 1G 107, the distributor 14 of the top of the tower internals 15 at middle part be connected to be arranged on 1 side wall of reaction tower into
Material mouth 1C 103；
The bed course 18 is five laminates that quartz sand or porcelain ball are combined into variable grain degree, and described five layer by layer
Shape structure is Pyatyi gradation: i.e. top layer's granularity close to or slightly larger than the catalyst granularity, undermost
Granularity is slightly larger than the gap dimension of the flase floor 19, between three layers from top to bottom, by small gradually big, upper and lower granularity linking arrangement,
Every thickness degree is in 5~15cm；It is to allow liquid phase fluid to pass through, and retain catalyst in tubulation 17 and expose that it, which is acted on,；Flase floor 19
Play the role of supporting bed course 18；
The demister 13, distributor 14, flase floor 19, material are all stainless steels；
Heating liquid import 1D 104 and heating liquid outlet 1F 106 are equipped in each section of catalytic section；
The module catalyst 40, structure is with the module catalyst in patent 201620189729.2: including catalyst, gold
Belong to silk screen 402, wire mesh corrugated plating 403, the module catalyst 40 is by the wire mesh 402, wire mesh ripple
The spaced and parallel setting of plate 403 installs the catalyst granules between wire mesh 402 described in two panels and forms catalyst layer 401
And the catalyst granules in the catalyst layer 401 by the wire mesh corrugated plating 403 apart from；The module
The catalyst layer 401 in catalyst 40 is spaced setting；
Catalyst in the module catalyst 40 is highly acidic resin catalyst, high temperature resistant strong acid resin catalyst, bears
Carry the superpower acid resin catalyst of metal；It is preferred that spherical or pearl highly acidic resin catalyst, high temperature resistant strong resin are catalyzed
The superpower acid resin catalyst of agent or carried metal；The type of carried metal is the main group II and VIII group member of the periodic table of elements
Element, load capacity are the 1-20% of resin catalyst exchange capacity；
The azeotropic catalytic tower, being added to the dehydrating agent in it from feed pump is dichloroethanes, benzene, aromatic hydrocarbons, ring
Any one in hexane or two kinds or more the mixtures being mixed in any proportion；
The azeotropic catalytic tower, for the tower internals 15 in tower if structured packing, filling number of segment is N, 1≤N≤
100, every section of height is 1-3 meters；Distributor 14, flase floor 19 are equipped between every section；If column plate, then number of theoretical plate is M, 1
The top of≤M≤100, tower is equipped with demister 13；
The catalytic section of the azeotropic catalytic tower, that is, tubulation bed section, the design number of segment of catalytic section are N, 1≤N≤10；
Distributor 14, bed course 18, flase floor 19 are equipped between every section；
Every section of 17 pipe number of tubulation is F, 1≤F≤10x104；Every root canal diameter is E, 2≤E≤30cm.
The return tank I 3, is equipped with inlet, leakage fluid dram and discharge outlet, and inside is equipped with coalescer 4；Wherein, inlet
It is connected with the outlet of condenser I 2, leakage fluid dram is mutually connected with the pump inlet of reflux pump I 5, discharge outlet and wastewater treatment system
System is connected, and gas phase forms liquid phase after condenser I condensation, into after in return tank I, is layered in coalescer and static state dual
The water taken off is discharged by discharge outlet under effect.
The finished product rectifying column 8, side wall lower section are installed on reboiler 9.
In the present invention, the condenser I, return tank I, coalescer, reflux pump I, heater, feed pump, finished product rectifying
Tower, reboiler, condenser II, return tank II, reflux pump II are this field commercial product, or the routine with corresponding function produces
Product.
The present invention also provides a kind of methods that azeotropic is catalyzed reaction synthesizing triformol, comprising the following steps:
(1) azeotropic dehydration: reach azeotropic temperature, water and part after formalin, dehydrating agent are heated to 50-100 DEG C
Dehydrating agent becomes gas phase to achieve the purpose that water export formaldehyde is concentrated, and the mixture formed after dehydration is the formalin of concentration
Solution and a small amount of unvaporized dehydrating agent；And the water of gas phase and partially dehydrated dose formed after being condensed, being coalesced liquid phase water and
The dehydrating agent of liquid phase, the water discharge of liquid phase, the dehydrating agent of liquid phase recycle；
(2) polymerization reaction: the mixture formed in step (1), the formalin of concentration therein, catalyst A's
Polymerization reaction is carried out under catalytic action and generates metaformaldehyde aqueous solution, and after polymerization reaction, product is metaformaldehyde aqueous solution
With a small amount of unvaporized dehydrating agent；
(3) finished product is fractionated: the product formed in step (2) is fractionated in a heated state, obtains gas phase and liquid phase；
Gas phase is dehydrating agent and a small amount of water present in product, is back in step (1) and follows through the reflux of condensation rear portion, a part
Ring utilizes, and liquid phase is product metaformaldehyde finished product, harvesting.
The present invention is illustrated below with reference to specific embodiment:
Embodiment 1:
A kind of method of azeotropic catalysis reaction synthesizing triformol, comprising the following steps:
(1) azeotropic dehydration: first by feed pump 7 by 50% formalin 100g and 80g dichloroethanes (dehydrating agent)
It imports in heater 6, normal heating enters the azeotropic dehydration in azeotropic catalytic tower 1 by feed inlet 1C to after 70-75 DEG C
Section, since this temperature is exactly the azeotropic temperature of dichloroethanes and water, the water for having azeotropic component is gasified and is risen to
Gaseous phase outlet 1A, i.e., 10% water and the dichloroethanes of 50g successively pass through condenser I 2, return tank I 3, reflux pump I 5,
The dichloroethanes of 50g or so is returned in azeotropic catalytic tower 1 by the first reflux liquid inlet mouth 1B and is recycled, moisture therein
It is separated under the action of return tank I is in coalescer 4, sewage disposal system is expelled to by the discharge outlet at the bottom return tank I；It is remaining
The unvaporized dichloroethanes of 30g can be continued traveling downwardly with the formalin of enrichment to 60%, be come in tubulation bed.
(2) polymerization reaction: under the catalytic action of resin catalyst of the formalin that concentration is 60% in tubulation, altogether
The hot water temperature of tubulation bed carries out polymerization reaction under 98-100 DEG C, normal pressure state in boiling catalytic tower, obtains the polymerization of 80g
Mix products, wherein 50g is metaformaldehyde (probably containing the water of 2g or so), and 30g is dichloroethanes；It polymerize mix products gradually
Tower bottom is fallen into, be discharged by discharge port 1E and continues to import in finished product rectifying column 8 by feed inlet 8A.
(3) finished product is fractionated: polymerization mix products are under the heating condition of reboiler 9, the dichloroethanes and water quilt of 32g or so
Be evaporated to gaseous phase outlet 8C, be successively divided into three tunnels after condenser II 10, return tank II 11, reflux pump II 12, all the way from
Refluxing opening 8B flows back 6.4g (reflux ratio 0.2) into finished product rectifying column, and another way 20g dichloroethanes is from the second reflux liquid inlet mouth
1G is back to recycling in tubulation bed, and in addition 5.6g dichloroethanes by the first reflux liquid inlet mouth 1B returns to azeotropic dehydration section all the way
In recycle, obtain the metaformaldehyde of 48g in tower bottom；The operating condition of finished product rectifying column is: 70-90 DEG C of tower top temperature,
0.1MPa, 80-120 DEG C of bottom temperature, 0.15MPa.
In the present embodiment, the yield of finished product reaches 95 or more %, purity is nearly 100%.
In the present embodiment, the resin catalyst filled in tubulation is the module catalyst that active constituent is D006；
In the present embodiment, the design of azeotropic catalytic tower 1 is as follows: tubulation bed is two sections, 1m every section high, every section totally 3
Tubulation 17, tubulation diameter are 5cm, are equipped with distributor 14, bed course 18, flase floor 19 from top to bottom between every section.Azeotropic dehydration section
It for structured packing, and is two sections, every section of height 1m, every section is equipped with distributor 14, flase floor 19 from top to bottom, and tower topmost exports
Place is equipped with demister 13.Demister, distributor, structured packing, material are made of stainless steel；
In the present embodiment, the bed course material is porcelain ball.
Embodiment 2:
A kind of method that azeotropic catalyzes and synthesizes metaformaldehyde, method and step is same as Example 1, except that first
The inlet amount of aldehyde aqueous solution and dichloroethanes increases 1 times, and tubulation bed 16 is set as one section, 1m every section high, every section totally 3 tubulation
17,17 diameter of tubulation is 5cm.It is nearly 100% that the yield of finished product, which remains at 95% or so, purity,.
Examples detailed above is technical conception and technical characteristics to illustrate the invention, can not be limited with this of the invention
Protection scope.The equivalent transformation or modification that all essence according to the present invention is done, should all cover in protection scope of the present invention
Within.
Claims (10)
1. a kind of method of azeotropic catalysis reaction synthesizing triformol, which comprises the following steps:
(1) azeotropic dehydration: reaching azeotropic temperature after formalin, dehydrating agent are heated to 50-100 DEG C, water and partially dehydrated
Agent becomes gas phase to achieve the purpose that water export formaldehyde is concentrated, and the mixture formed after dehydration is the formalin of concentration
With a small amount of unvaporized dehydrating agent；And the water of gas phase and partially dehydrated dose form the water and liquid phase of liquid phase after being condensed, being coalesced
Dehydrating agent, the water discharge of liquid phase, the dehydrating agent of liquid phase recycles；
(2) polymerization reaction: the mixture formed in step (1), the formalin of concentration therein, in the catalysis of catalyst A
Polymerization reaction is carried out under effect and generates metaformaldehyde aqueous solution, and after polymerization reaction, product is for metaformaldehyde aqueous solution and less
The unvaporized dehydrating agent of amount；
(3) finished product is fractionated: the product formed in step (2) is fractionated in a heated state, obtains gas phase and liquid phase；Gas phase
For dehydrating agent present in product and a small amount of water, circulation benefit in step (1) is back to through the reflux of condensation rear portion, a part
With liquid phase is product metaformaldehyde finished product, harvesting.
2. the method according to claim 1, wherein method specifically includes the following steps:
(1) azeotropic dehydration: formalin, dehydrating agent are imported into the tube side of heater (6) by feed pump (7) and are heated,
Reach azeotropic temperature after being heated to 50-100 DEG C under the conditions of normal pressure or micro-positive pressure, azeotropic catalysis reaction is imported by feed inlet 1C
Azeotropic dehydration is carried out in the azeotropic dehydration section of tower (1), achievees the purpose that formaldehyde, under the action of azeotropic principles, shape in tower is concentrated
At two-phase: gas phase is water and partially dehydrated dose, and liquid phase is the formalin and a small amount of unvaporized dehydration after dehydration concentration
Agent；Wherein: gas phase rises to tower top and is discharged from gaseous phase outlet 1A, and water and the dehydration of liquid phase are formed after condenser I (2) condensation
Agent, the water and dehydrating agent of liquid phase are under the double action of coalescer (4) and static layering in return tank I by the water taken off by arranging
Mouth of a river discharge, the dehydrating agent of liquid phase are then refluxed pump I and are pumped to the first refluxing opening 1B to infinite reflux to azeotropic catalytic tower
In recycle；And it is dehydrated the formalin after concentration and a small amount of unvaporized dehydrating agent, under gravity under meeting
Row is into the catalytic section of azeotropic catalytic tower (1)；
(2) polymerization reaction: the formalin after dehydration concentration comes downwards in the tubulation bed of catalytic section, the catalyst in tubulation
Catalytic action under carry out polymerization reaction generate metaformaldehyde aqueous solution, after polymerization reaction, product be metaformaldehyde it is water-soluble
Liquid and a small amount of unvaporized dehydrating agent；Product is continued traveling downwardly under the effect of gravity to tower bottom, be discharged by discharge port 1E and by into
Material mouth 8A is imported into finished product rectifying column (8)；The heating liquid import 1D of catalytic section is connected with heat-exchanger pump, the heat that heat-exchanger pump provides
Water enters in the shell side of catalytic section, provides temperature, heating liquid outlet 1F and hot-water collection system for the polymerization reaction in tubulation
It is connected；
(3) finished product is fractionated: after the product formed in step (2) imported into finished product rectifying column (8), in the heating shape of reboiler (9)
It is fractionated under state, obtains gas phase and liquid phase；Gas phase is dehydrating agent and a small amount of water present in product, is arranged through gaseous phase outlet 8C
It out and enters in condenser II (10) and is condensed, the dehydrating agent and a small amount of water condensed is followed by return tank II
(11), it is divided into three tunnels after reflux pump II (12), is connected all the way with refluxing opening 8B, the first reflux of another way and azeotropic catalytic tower
Inlet 1B is connected, and third road is connected with the second reflux liquid inlet mouth 1G that tubulation bed lowest part distributor is connected to, continue into
Enter into tubulation bed and is persistently dehydrated and recycles；The pure metaformaldehyde product of the obtained liquid phase, that is, finished product of tower bottom, by going out
Material mouth 8D discharge is collected.
3. according to the method described in claim 2, the formaldehyde it is characterized in that, in step (1), in dehydrating agent and formalin
Mass ratio be 1-10:1；The mass fraction of formaldehyde is 30-55% in formalin；The dehydrating agent be purified petroleum benzin, aromatic hydrocarbons,
Any one in dichloroethanes, hexamethylene or two kinds or more the mixtures being mixed in any proportion.
4. according to the method described in claim 2, it is characterized in that, the catalyst is highly acidic resin catalysis in step (2)
The superpower acid resin catalyst of agent, high temperature resistant strong acid resin catalyst or carried metal；The heat-exchanger pump, the hot water provided
Temperature is 80-120 DEG C, guarantees that the temperature of polymerization reaction in tubulation bed is 70-110 DEG C.
5. according to the method described in claim 2, it is characterized in that, in step (3), the finished product rectifying column (8) operates item
Part are as follows: tower top temperature: 30-110 DEG C；Column bottom temperature: 80-180 DEG C；Operating pressure: 0.01-1.5Mpa；Condense obtained dehydration
Agent and a small amount of water are back in finished product rectifying column from refluxing opening 8B, reflux ratio 0.1-2.0.
6. a kind of device of azeotropic catalysis reaction synthesizing triformol, including feed pump (7), the heater (6), altogether being sequentially connected
Catalytic tower (1), finished product rectifying column (8) are boiled, raw material formalin and dehydrating agent are first into the tube side of heater (6)
Interior heating, then into being dehydrated in azeotropic catalytic tower, the result of dehydration is divided into two-phase: gas phase ascends into azeotropic
Dewatering period and flow out outside tower, liquid phase falls under gravity into catalytic section and carries out polymerization reaction；Polymerizate imported into essence
It evaporates in tower (8), obtains product metaformaldehyde finished product after being fractionated；It is characterized by:
The feed pump (7), be equipped with import 7A and outlet 7B, in which: import 7A and be capable of providing raw material formalin with
The device of dehydrating agent is connected；
The heater (6) is equipped with import 6A and outlet 6B, in which: import 6A is connected with the outlet 7B of feed pump；
The azeotropic catalytic tower (1), top is equipped with gaseous phase outlet 1A (101), bottom is equipped with discharge port 1E (105), side
The top of wall is equipped with the first reflux liquid inlet mouth 1B (102), middle part is equipped with feed inlet 1C (103), middle and lower part is equipped with the outlet of heating liquid
1F (106) and heating liquid import 1D (104), lower part are equipped with the second reflux liquid inlet mouth 1G (107), and the position for heating liquid import 1D is low
1F is exported in heating liquid；Wherein: feed inlet 1C is connected with the outlet 6B of heater (6)；Gaseous phase outlet 1A is connected in turn cold
Condenser I (2), return tank I (3) and reflux pump I (5), the pump discharge of reflux pump I are connected with the first reflux liquid inlet mouth 1B；Heating
Liquid import 1D is connected with heat-exchanger pump, and heating liquid outlet 1F is connected with hot-water collection system；
The return tank I (3), is equipped with inlet, leakage fluid dram and discharge outlet, and inside is equipped with coalescer (4)；Wherein, inlet
It is connected with the outlet of condenser I (2), leakage fluid dram is mutually connected with the pump inlet of reflux pump I (5), discharge outlet and wastewater treatment
System is connected, and gas phase forms liquid phase after condenser I condensation, into after in return tank I, in pair of coalescer and static layering
Recast is discharged with the lower water that will be taken off by discharge outlet；
The finished product rectifying column (8), top is equipped with gaseous phase outlet 8C, bottom is equipped with finished product discharge port 8D, is equipped with above side wall
Refluxing opening 8B, middle part are equipped with feed inlet 8A, in which: feed inlet 8A is connected with the discharge port 1E of azeotropic catalytic tower；Gas phase
Outlet 8C is connected with condenser II (10), return tank II (11) and reflux pump II (12) in turn；The pump discharge of reflux pump (12) point
For three tunnels, it is connected all the way with refluxing opening 8B, another way is connected with the first reflux liquid inlet mouth 1B of azeotropic catalytic tower, third road
It is connected with 1G mouthfuls of the second reflux liquid inlet mouth of azeotropic catalytic tower, continues into azeotropic catalytic tower and be persistently dehydrated and recycle benefit
With；Discharge port 8D is connected with the device for acquiring or receiving finished product metaformaldehyde；
The finished product rectifying column (8), side wall lower section are installed on reboiler (9).
7. device according to claim 6, which is characterized in that the azeotropic catalytic tower (1), interior top are equipped with and remove
Foam device (13), demister (13) lower section include the catalytic section of superposed azeotropic dehydration section and lower part, and the azeotropic is de-
The top of water section sets gradually distributor (14), flase floor (19) from top to bottom；The top of the catalytic section is from top to bottom successively
Distributor (14), flase floor (19) are set, and the bottom of the catalytic section is successively arranged distributor (14), bed course from top to bottom
(18), flase floor (19)；The azeotropic dehydration section be equipped with tower internals (15), the tower internals (15) be include structured packing or tower
Any one in plate；It includes structured packing that the tower internals (15), which is selected, and the structured packing loads number of segment as N, and 1≤N
≤ 100, every section of height is to be equipped with distributor (14), flase floor (19) between 1-3 meters, each section, and the distributor (14) is in institute
It states on flase floor (19)；Or it includes column plate that the tower internals (15), which is selected, the number of plates is M, 1≤M≤100；It is described
Catalytic section includes tubulation bed (16), and the number of segment of the catalytic section is N, 1≤N≤10, is successively arranged from top to bottom between each section point
Cloth device (14), bed course (18), flase floor (19)；
The tubulation bed (16) includes the more tubulations being vertically arranged (17), fills module catalyst (40) in the tubulation (17), institute
It states between tubulation (17) outer wall and reaction tower (1) inner wall to heat liquid stream road, is all provided at the top and bottom of the tubulation bed (16)
Fluid conduit upper and lower side closure will be added by setting closed guard, and the baffle is equipped with the corresponding tubulation of multiple open communications (17) both ends
Opening；The reaction raw materials that the azeotropic dehydration section flows down sequentially pass through each distributor (14) in catalytic section described in multistage,
Bed course (18), flase floor (19), tubulation (17) discharge；
Discharge port 1E (105) are equipped with equipped with gaseous phase outlet 1A (101), bottom at the top of the azeotropic catalytic tower (1), it is described anti-
It answers and is located at tubulation bed (16) bottom setting heating liquid import 1D (104), the heating liquid import 1D on tower (1) side wall
(104) opposite side is located at setting heating liquid outlet 1F at the top of tubulation bed (16) on azeotropic catalytic tower (1) side wall
(106), the distributor (14) of azeotropic catalytic tower (1) topmost is connected to the first reflux liquid inlet mouth being arranged on its side wall
1B (102), lowest part distributor (14) be connected to the second reflux liquid inlet mouth 1G (107) being arranged on its side wall, middle part it is described
Distributor (14) above tower internals (15) is connected to the feed inlet 1C (103) being arranged on azeotropic catalytic tower (1) side wall.
8. device according to claim 7, which is characterized in that the bed course (18) is quartz sand or porcelain ball with different
Combinations of particle sizes at five laminates, five laminate is Pyatyi gradation: i.e. top layer's granularity close to or
Slightly larger than the granularity of the catalyst, undermost granularity is slightly larger than the gap dimension of the flase floor (19), Zhi Jiansan
From top to bottom, by small gradually big, upper and lower granularity linking arrangement, every thickness degree is in 5~15cm for layer；The demister (13), distributor
(14), flase floor (19), material are all stainless steels.
9. device according to claim 7, which is characterized in that be equipped with heating liquid import 1D in each section of catalytic section
(104) and heating liquid exports 1F (106)；The module catalyst (40), including catalyst, wire mesh (402), wire mesh
Corrugated plating (403), the module catalyst (40) are spaced flat by the wire mesh (402), wire mesh corrugated plating (403)
Row is arranged, and the catalyst granules is installed between wire mesh (402) described in two panels and forms catalyst layer (401), and this is urged
The catalyst granules in agent layer (401) by the wire mesh corrugated plating (403) apart from；The module is urged
The catalyst layer (401) in agent (40) is spaced setting.
10. device according to claim 7, which is characterized in that the catalyst in module catalyst (40) is highly acid tree
Rouge catalyst, high temperature resistant strong acid resin catalyst, carried metal superpower acid resin catalyst；It is added to azeotropic from feed pump to urge
Changing the dehydrating agent in reaction tower is dichloroethanes, benzene, aromatic hydrocarbons, any one or two kinds or more in hexamethylene arbitrarily to compare
The mixture that example mixes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811358845.2A CN109369607B (en) | 2018-11-15 | 2018-11-15 | Device and method for synthesizing trioxymethylene through azeotropic catalytic reaction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811358845.2A CN109369607B (en) | 2018-11-15 | 2018-11-15 | Device and method for synthesizing trioxymethylene through azeotropic catalytic reaction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109369607A true CN109369607A (en) | 2019-02-22 |
| CN109369607B CN109369607B (en) | 2023-08-01 |
Family
ID=65389291
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811358845.2A Active CN109369607B (en) | 2018-11-15 | 2018-11-15 | Device and method for synthesizing trioxymethylene through azeotropic catalytic reaction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109369607B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109851501A (en) * | 2019-03-20 | 2019-06-07 | 江苏索普（集团）有限公司 | Ethyl acetate integration system is for tower |
| CN110156747A (en) * | 2019-04-16 | 2019-08-23 | 天津大学 | A kind of partition wall reactive distillation manufacturing technique method and device for metaformaldehyde |
| CN114478475A (en) * | 2022-03-14 | 2022-05-13 | 凯瑞环保科技股份有限公司 | Process and device for synthesizing trioxymethylene |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4962235A (en) * | 1988-04-07 | 1990-10-09 | Asahi Kasei Kogyo Kabushiki Kaisha | Process for producing high purity formaldehyde |
| CN106831380A (en) * | 2017-01-19 | 2017-06-13 | 中国科学院成都有机化学有限公司 | The method of formalin dehydration concentration |
| CN108329294A (en) * | 2018-04-10 | 2018-07-27 | 中国科学院成都有机化学有限公司 | Formaldehyde prepares the coupling process of metaformaldehyde |
| CN108395422A (en) * | 2018-05-16 | 2018-08-14 | 凯瑞环保科技股份有限公司 | A kind of the synthesis extracting process and device of metaformaldehyde |
-
2018
- 2018-11-15 CN CN201811358845.2A patent/CN109369607B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4962235A (en) * | 1988-04-07 | 1990-10-09 | Asahi Kasei Kogyo Kabushiki Kaisha | Process for producing high purity formaldehyde |
| CN106831380A (en) * | 2017-01-19 | 2017-06-13 | 中国科学院成都有机化学有限公司 | The method of formalin dehydration concentration |
| CN108329294A (en) * | 2018-04-10 | 2018-07-27 | 中国科学院成都有机化学有限公司 | Formaldehyde prepares the coupling process of metaformaldehyde |
| CN108395422A (en) * | 2018-05-16 | 2018-08-14 | 凯瑞环保科技股份有限公司 | A kind of the synthesis extracting process and device of metaformaldehyde |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109851501A (en) * | 2019-03-20 | 2019-06-07 | 江苏索普（集团）有限公司 | Ethyl acetate integration system is for tower |
| CN110156747A (en) * | 2019-04-16 | 2019-08-23 | 天津大学 | A kind of partition wall reactive distillation manufacturing technique method and device for metaformaldehyde |
| CN110156747B (en) * | 2019-04-16 | 2023-05-23 | 天津大学 | Separation wall reaction rectification production process method and device for trioxymethylene |
| CN114478475A (en) * | 2022-03-14 | 2022-05-13 | 凯瑞环保科技股份有限公司 | Process and device for synthesizing trioxymethylene |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109369607B (en) | 2023-08-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103012062B (en) | Process for indirectly producing alcohol with synthetic gas and application of process | |
| CN109369607A (en) | A kind of device and method of azeotropic catalysis reaction synthesizing triformol | |
| US8551295B2 (en) | Reactive distillation apparatus for a multistage counter-current rotating bed and its application | |
| CN106957221A (en) | The device and method of polymethoxy dimethyl ether is produced in a kind of methanol oxidation | |
| CN108409707A (en) | A kind of the catalytic distillation synthetic method and device of metaformaldehyde | |
| CN105061165B (en) | Reaction apparatus for preparing polyoxymethylene dimethyl ether | |
| CN203033918U (en) | Process system for indirectly producing ethanol by using synthesis gases | |
| CN106117013A (en) | The method of purification of a kind of 1,3 propylene glycol and device thereof | |
| CN209508105U (en) | A kind of device of azeotropic catalysis reaction synthesizing triformol | |
| CN209378964U (en) | Azeotropic catalytic tower | |
| CN106631739A (en) | Crotonaldehyde reaction rectification production method and device based on solid alkali | |
| CN105622366B (en) | A kind of device and method for producing polymethoxy dimethyl ether DMM3 5 | |
| CN100569725C (en) | Formaldehyde absorbing method and system | |
| CN107721831A (en) | A kind of polymethoxy dimethyl ether synthesizes the plug-in reaction system of bubble type and synthetic method | |
| CN206814664U (en) | The device of polymethoxy dimethyl ether is produced in a kind of methanol oxidation | |
| CN109232202A (en) | A kind of one-step synthesis method DMM3-8Device and method | |
| CN208814917U (en) | A kind of formaldehyde reacts the catalytic rectifying tower for producing dimethoxym ethane with methanol | |
| JPS5898101A (en) | Gas-liquid contact apparatus | |
| CN109277056B (en) | Azeotropic catalytic reaction tower | |
| CN109180636B (en) | Device and method for synthesizing trioxymethylene by coupling extraction and catalysis technology | |
| CN109232516A (en) | A kind of multifunctional membrane synthesizing triformol and DMM3-8Device and method | |
| CN210261603U (en) | N-methyldiethanolamine production device | |
| CN204447369U (en) | A kind of tandem heater of acrylic acid dehydrating tower | |
| CN105348113B (en) | N-(1-ethyl propyl)-3,4-dimethylaniline continuous production device and method | |
| CN209493513U (en) | A kind of multifunctional membrane synthesizing triformol and DMM3-8Device |
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 |