CN206188684U - Reduce device that propylene carbonylation process central plain material consumed - Google Patents
Reduce device that propylene carbonylation process central plain material consumed Download PDFInfo
- Publication number
- CN206188684U CN206188684U CN201621051799.8U CN201621051799U CN206188684U CN 206188684 U CN206188684 U CN 206188684U CN 201621051799 U CN201621051799 U CN 201621051799U CN 206188684 U CN206188684 U CN 206188684U
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- pipeline
- cooler
- propylene
- flash tank
- 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.)
- Withdrawn - After Issue
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a reduce device that propylene carbonylation process central plain material consumed, the heat exchanger is connected at second carbonyl synthesis reactor top, the gas output port at heat exchanger top and high pressure evaporator collecting vat top all is linked together with heat exchanger's shell side entry, heat exchanger's shell side export connects gradually electric heating furnace, fixed bed reactor and first cooler, a cooler outlet is connected with heat exchanger's tube side import, the export of heat exchanger tube side connects gradually second cooler, the compressor, air cooler and flash tank, the flash tank top is linked together with synthetic gas input pipeline, the flash tank bottom is connected with depropanizator, the depropanizator top is linked together with propylene input pipeline, the depropanizator bottom is linked together with heat exchanger's shell side import. The utility model provides a discharge a large amount of industrial waste gas's problem in the production process, reach the environmental protection requirement to the standard of environment zero release, reduce the raw material consumption among the industrial process.
Description
Technical field
The utility model is related to a kind of device, is to be related to raw material during a kind of reduction propenecarbonyl in particular
The device of consumption.
Background technology
Domestic industry produces the device of octyl alconyl, and most of is all using the second generation propylene rhodium method low pressure carbonyl of DAVY/DDW
Base synthesizes --- liquid phase circulation technology.The reaction raw materials of the carbonylation synthesis are mainly propylene and synthesis gas, are first propylene
With synthesis gas by purifying, carbongl group synthesis reaction system is then delivered to, in carbonyl synthesis reactor system inner propene and synthesis gas
There is carbonylation in the presence of homogeneous catalyst, generate butyraldehyde.The butyraldehyde of generation enters high with catalyst mother liquor
Removing light component (propylene, propane, synthesis gas etc.) is carried out in pressure evaporator.But propylene can be sent out during it there is carbonyl reaction
There is addition reaction in the side reaction of first portion, such as propylene, generate propane with the hydrogen in synthesis gas.With the hair of side reaction
Raw, the amount of the propane of generation gradually increases, and inert gas is acting as during the course of the reaction, therefore will be anti-from carbonylation synthesis
Answer and discharged at the top of device, while the gas being evaporated from high pressure evaporator is with the release at the top of carbonyl synthesis reactor
Gas is carried out in emptying feeding fuel gas house steward in the lump.Wherein the content of propane can reach more than 43.2% in this portion gas,
The content of propylene reaches 17.5%, the content about 14.8% of hydrogen, and the content of carbon monoxide reaches 4.4%.Therefore fuel is entered
Available gas in gas house steward reach more than 80%, if this gas recycled, will substantially reduce propenecarbonyl
During consumption of raw materials.
Utility model content
The purpose of this utility model is to overcome deficiency of the prior art, there is provided one kind reduces propenecarbonyl process
The device of middle consumption of raw materials, solves the problems, such as to discharge big capacity industrial waste gas in production process, reaches the mark to environment zero-emission
Accurate environmental requirement, reduces the consumption of raw materials in industrial processes.
The purpose of this utility model is achieved through the following technical solutions.
The device of consumption of raw materials during a kind of reduction propenecarbonyl of the present utility model, including first for being sequentially connected
Carbonyl synthesis reactor, the second carbonyl synthesis reactor and high pressure evaporator collecting tank, first carbonyl synthesis reactor connect
Propylene intake pipeline and synthesis gas intake pipeline are connected to, the second carbonyl synthesis reactor top is connected with heat exchanger, described
Gas delivery port at the top of heat exchanger top and high pressure evaporator collecting tank passes through the shell side inlet phase of pipeline and heat exchanger
Connection, the shell-side outlet of the heat exchanger is connected with electric furnace, fixed bed reactors and the first cooling in turn by pipeline
Device, the outlet of first cooler is connected with the tube side import of heat exchanger, and the tube side outlet of the heat exchanger passes through
Pipeline is connected with the second cooler, compressor, air cooler and flash tank in turn, and the flash drum overhead passes through hydrogen delivery tube line
It is connected with synthesis gas intake pipeline, the flash tank bottom is connected with depropanizing tower, the depropanizing tower top passes through pipeline
It is connected with propylene intake pipeline, the depropanizing tower bottom is connected by pipeline with the shell side import of heat exchanger.
The hydrogen delivery tube line is communicated with carbon monoxide and allocates pipeline into.
Compared with prior art, the beneficial effect that the technical solution of the utility model is brought is：
In the utility model, the release gas of the second carbonyl synthesis reactor and the release gas of high pressure evaporator collecting tank are together
Input heat exchanger shell side carries out once heat and changes, and secondary heat exchange is carried out into electric furnace, into fixed bed reactors, is taken off
Hydrogen reacts, and after being exchanged heat into the tube side of heat exchanger through the first cooler, is exchanged heat through the second cooler and lowered the temperature, and is delivered to pressure
Be compressed in contracting machine, by after air cooler cooling, separating in the flash tank, the hydrogen of flash drum overhead discharge with allocate into
Carbon monoxide is delivered in the first carbonyl synthesis reactor together, and the material of flash tank bottom discharge is delivered to depropanizing tower, takes off
The propylene of propane top of tower discharge is delivered in the first carbonyl synthesis reactor, the propane reflux of depropanizing tower bottom discharge to heat
In the shell side of exchanger, it is thusly-formed and recycles, solve the problems, such as to discharge big capacity industrial waste gas in production process, it is right to reach
The environmental requirement of the standard of environment zero-emission, reduces the consumption of raw materials in industrial processes, cost-effective.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model.
Reference:1 first carbonyl synthesis reactor；2 second carbonyl synthesis reactors；3 propylene intake pipelines；4 synthesis
Gas intake pipeline；5 nitrogen intake pipelines；6 first outer loop water coolers；7 second outer loop water coolers；8 heat exchangers；
10 high pressure evaporators；11 high pressure evaporator collecting tanks；13 low pressure evaporators；14 separators；15 points of liquid baths；16 cymogene aldehyde are collected
Groove；17 heat exchangers；18 electric furnaces；19 fixed bed reactors；20 first coolers；21 second coolers；22 compressors；23
Air cooler；24 flash tanks；25 hydrogen delivery tube lines；26 depropanizing towers；27 carbon monoxide allocate pipeline into.
Specific embodiment
The utility model will be further described below in conjunction with the accompanying drawings.
As shown in figure 1, a kind of device for reducing consumption of raw materials during propenecarbonyl of the invention, including is connected with third
First carbonyl synthesis reactor 1 of alkene intake pipeline 3 and synthesis gas intake pipeline 4, the propylene intake pipeline 3 and synthesis gas are defeated
Enter pipeline 4 and be communicated with nitrogen intake pipeline 5, wherein, from commercial plant and by purification, synthesis gas is mainly comprising next for propylene
From the carbon monoxide and hydrogen of commercial plant, and by purification, nitrogen intake pipeline 5 is closed with the pressure of 10MPa to the first carbonyl
The supplying nitrogen into reactor 1.Material at the top of first carbonyl synthesis reactor 1 out and the purification from commercial plant
Synthesis gas enters in the second carbonyl synthesis reactor 2 together, carries out carbonylation；The bottom of first carbonyl synthesis reactor 1
Portion's material out is divided into two parts, after a part is cooled down through the first outer loop water cooler 6, is returned by propylene input port
To the first carbonyl synthesis reactor 1, reaction system in the first carbonyl synthesis reactor 1 is lowered the temperature, another part and second
The bottom of carbonyl synthesis reactor 2 out through the second outer loop water cooler 7 cool down after material together enter the second carbonyl
In synthesis reactor 2, carry out secondary response again and ensure the temperature stabilization in the second carbonyl synthesis reactor 2.Second carbonyl
The top gas phase material of synthesis reactor 2 is cooled down into the tube side of heat exchanger 8, and the condensate liquid after cooling is back to the second carbonyl downwards
Reaction is continued to participate in base synthesis reactor 2, fixed gas is discharged from gas delivery port upwards along tube side, wherein, the heat exchange
The shell side of device 8 is passed through cooling water.A part of material of the bottom of the second carbonyl synthesis reactor 2 enters high pressure evaporator 10
It is interior, the heated rear light component (propylene, methane, synthesis gas) entered in the Removal of catalyst mixed liquor of high pressure evaporator collecting tank 11
Deng, the material after light component from the bottom of high pressure evaporator collecting tank 11 outflow has been removed, heated into low pressure evaporator 13
Flash separation is carried out into separator 14 afterwards, catalyst mother liquor reflux to the interior circulation of the first carbonyl synthesis reactor 1 of bottom makes
With, the top of the separator 14 abjection butyraldehyde, condensed butyraldehyde enters a point liquid bath 15, subsequently into cymogene aldehyde collecting tank 16,
From the discharge of the bottom of cymogene aldehyde collecting tank 16, uncooled cymogene aldehyde is discharged from the top of point liquid bath 15.
The gas delivery port at the top of the high pressure evaporator collecting tank 11 and the top of heat exchanger 8 passes through pipeline and heat exchange
The shell side inlet of device 17 is connected, and the shell-side outlet of the heat exchanger 17 is connected with electric furnace 18 in turn, consolidates by pipeline
The cooler 20 of fixed bed reactor 19 and first, the outlet of first cooler 20 is connected with the tube side import of heat exchanger 17
Connect.The tube side outlet of the heat exchanger 17 is connected with the second cooler 21, compressor 22, the and of air cooler 23 in turn by pipeline
Flash tank 24, the top of the flash tank 24 is connected by hydrogen delivery tube line 25 with synthesis gas intake pipeline 4, and the hydrogen is defeated
Send pipeline 25 to be communicated with carbon monoxide and allocate pipeline 27 into, the bottom of the flash tank 24 is connected with depropanizing tower 26, the depropanization
The top of tower 26 is connected by pipeline with propylene intake pipeline 3, and the bottom of the depropanizing tower 26 is by pipeline and heat exchanger 17
Shell side import be connected.According to actual needs, the gas at the top of the high pressure evaporator collecting tank 11 and the top of heat exchanger 8 is defeated
Outlet can connection flow gauge.
The method of consumption of raw materials, comprises the following steps during reduction propenecarbonyl based on said apparatus：
First, by the release at the release gas at the top of the second carbonyl synthesis reactor 2 and the top of high pressure evaporator collecting tank 11
Gas is input into the shell side of heat exchanger 17 and carries out first time heat exchange together, the temperature of mixed material is reached 185 DEG C -225 DEG C, heat exchange
Mixed material afterwards carries out secondary heat exchange into electric furnace 18, in electric furnace 18 temperature of mixed material reach 590 DEG C-
605 DEG C, pressure reaches 0.05MPa-0.06MPa.
Then, it is ensured that the mixed material after secondary heat exchange into fixed bed reactors 19, is being urged under the conditions of gaseous
Agent Cr/Al2O3Dehydrogenation reaction is carried out in the presence of solid-carried catalyst, in the control of the interior reaction temperature of fixed bed reactors 19 590
DEG C -650 DEG C, Stress control is in 32KPa-49KPa.With the use of catalyst, the catalysis activity reduction of catalyst is properly increased
Reaction temperature, it is ensured that more than 70%, the selectivity of propylene is more than 93% for the conversion per pass of propane.
Secondly, in fixed bed reactors 19 through the mixed material after dehydrogenation reaction through the first cooler 20 be cooled to 360 DEG C-
After 380 DEG C, into the tube side of heat exchanger 17 in exchanged heat to 190 DEG C -200 DEG C.
Then, heat exchange cooling is carried out in from the mixed material of the tube side of heat exchanger 17 discharge into the second cooler 21, is dropped
To after 65 DEG C -75 DEG C, it is delivered in compressor 22, mixed material is compressed in the presence of compressor 22, the vapour of generation
State condensate, in being directly entered flash tank 24 after air cooler 23 is cooled to 35 DEG C -42 DEG C, separates in flash tank 24, dodges
The mainly uncooled hydrogen of the top discharge of steaming pot 24, is incorporated in synthesis gas intake pipeline 4, together with the carbon monoxide allocated into
It is delivered in the first carbonyl synthesis reactor 1.
Finally, the material of the bottom of flash tank 24 discharge after drying, is delivered to depropanizing tower 26, the top of depropanizing tower 26 third
Alkene purity can reach more than 99.5%, is incorporated in propylene intake pipeline 3 by pipeline, and the first carbongl group synthesis reaction is delivered to together
In device 1, in propane reflux to the shell side of heat exchanger 17 of the bottom discharge of depropanizing tower 26, recycling is circulated.
Embodiment one
During reduction propenecarbonyl of the invention in the method for consumption of raw materials, first, by the second carbongl group synthesis reaction
Release gas at the top of the release gas and high pressure evaporator collecting tank 11 at the top of device 2 is input into the shell side of heat exchanger 17 together carries out the
Once exchange heat, the temperature of mixed material is reached 185 DEG C, the mixed material after heat exchange carries out secondary changing into electric furnace 18
Heat, the temperature of mixed material reaches 590 DEG C in electric furnace 18, and pressure reaches 0.05MPa.
Then, it is ensured that the mixed material after secondary heat exchange into fixed bed reactors 19, is being urged under the conditions of gaseous
Agent Cr/Al2O3Dehydrogenation reaction is carried out in the presence of solid-carried catalyst, in the control of the interior reaction temperature of fixed bed reactors 19 590
DEG C, Stress control is in 32KPa.With the use of catalyst, the catalysis activity reduction of catalyst properly increases reaction temperature, protects
The conversion per pass of propane is demonstrate,proved more than 70%, the selectivity of propylene is more than 93%.
Secondly, 360 DEG C are cooled to through the first cooler 20 through the mixed material after dehydrogenation reaction in fixed bed reactors 19
Afterwards, into being exchanged heat to 190 DEG C in the tube side of heat exchanger 17.
Then, heat exchange cooling is carried out in from the mixed material of the tube side of heat exchanger 17 discharge into the second cooler 21, is dropped
To after 65 DEG C, it is delivered in compressor 22, mixed material is compressed in the presence of compressor 22, the steam state condensation of generation
Thing, in being directly entered flash tank 24 after air cooler 23 is cooled to 35 DEG C, separates in flash tank 24, the top of flash tank 24 row
The mainly uncooled hydrogen put, is incorporated in synthesis gas intake pipeline 4 with the carbon monoxide allocated into, and the first carbonyl is delivered to together
In base synthesis reactor 1.
Finally, the material of the bottom of flash tank 24 discharge after drying, is delivered to depropanizing tower 26, and the top of depropanizing tower 26 can
The propylene that purity is 99.5% is obtained, is incorporated in propylene intake pipeline 3 by pipeline, the first carbongl group synthesis reaction is delivered to together
In device 1, in propane reflux to the shell side of heat exchanger 17 of the bottom discharge of depropanizing tower 26, recycling is circulated.
Consumption of raw materials during propenecarbonyl can effectively be reduced using this method, one ton of butyraldehyde is often produced, propylene disappears
Consumption can reduce 5KG, and synthesis gas consumption can reduce 10NM3。
Embodiment two
During reduction propenecarbonyl of the invention in the method for consumption of raw materials, first, by the second carbongl group synthesis reaction
Release gas at the top of the release gas and high pressure evaporator collecting tank 11 at the top of device 2 is input into the shell side of heat exchanger 17 together carries out the
Once exchange heat, the temperature of mixed material is reached 200 DEG C, the mixed material after heat exchange carries out secondary changing into electric furnace 18
Heat, the temperature of mixed material reaches 600 DEG C in electric furnace 18, and pressure reaches 0.055MPa.
Then, it is ensured that the mixed material after secondary heat exchange into fixed bed reactors 19, is being urged under the conditions of gaseous
Agent Cr/Al2O3Dehydrogenation reaction is carried out in the presence of solid-carried catalyst, in the control of the interior reaction temperature of fixed bed reactors 19 620
DEG C, Stress control is in 40KPa.With the use of catalyst, the catalysis activity reduction of catalyst properly increases reaction temperature, protects
The conversion per pass of propane is demonstrate,proved more than 70%, the selectivity of propylene is more than 93%.
Secondly, 370 DEG C are cooled to through the first cooler 20 through the mixed material after dehydrogenation reaction in fixed bed reactors 19
Afterwards, into being exchanged heat to 195 DEG C in the tube side of heat exchanger 17.
Then, heat exchange cooling is carried out in from the mixed material of the tube side of heat exchanger 17 discharge into the second cooler 21, is dropped
To after 70 DEG C, it is delivered in compressor 22, mixed material is compressed in the presence of compressor 22, the steam state condensation of generation
Thing, in being directly entered flash tank 24 after air cooler 23 is cooled to 40 DEG C, separates in flash tank 24, the top of flash tank 24 row
The mainly uncooled hydrogen put, is incorporated in synthesis gas intake pipeline 4 with the carbon monoxide allocated into, and the first carbonyl is delivered to together
In base synthesis reactor 1.
Finally, the material of the bottom of flash tank 24 discharge after drying, is delivered to depropanizing tower 26, and the top of depropanizing tower 26 can
The propylene that purity is 99.53% is obtained, is incorporated in propylene intake pipeline 3 by pipeline, the first carbonylation synthesis are delivered to together anti-
Answer in device 1, in propane reflux to the shell side of heat exchanger 17 of the bottom discharge of depropanizing tower 26, be circulated recycling.
Consumption of raw materials during propenecarbonyl can effectively be reduced using this method, one ton of butyraldehyde is often produced, propylene disappears
Consumption can reduce 5.9KG, and synthesis gas consumption can reduce 12NM3。
Embodiment three
During reduction propenecarbonyl of the invention in the method for consumption of raw materials, first, by the second carbongl group synthesis reaction
Release gas at the top of the release gas and high pressure evaporator collecting tank 11 at the top of device 2 is input into the shell side of heat exchanger 17 together carries out the
Once exchange heat, the temperature of mixed material is reached 225 DEG C, the mixed material after heat exchange carries out secondary changing into electric furnace 18
Heat, the temperature of mixed material reaches 605 DEG C in electric furnace 18, and pressure reaches 0.06MPa.
Then, it is ensured that the mixed material after secondary heat exchange into fixed bed reactors 19, is being urged under the conditions of gaseous
Agent Cr/Al2O3Dehydrogenation reaction is carried out in the presence of solid-carried catalyst, in the control of the interior reaction temperature of fixed bed reactors 19 650
DEG C, Stress control is in 49KPa.With the use of catalyst, the catalysis activity reduction of catalyst properly increases reaction temperature, protects
The conversion per pass of propane is demonstrate,proved more than 70%, the selectivity of propylene is more than 93%.
Secondly, 380 DEG C are cooled to through the first cooler 20 through the mixed material after dehydrogenation reaction in fixed bed reactors 19
Afterwards, into being exchanged heat to 200 DEG C in the tube side of heat exchanger 17.
Then, heat exchange cooling is carried out in from the mixed material of the tube side of heat exchanger 17 discharge into the second cooler 21, is dropped
To after 75 DEG C, it is delivered in compressor 22, mixed material is compressed in the presence of compressor 22, the steam state condensation of generation
Thing, in being directly entered flash tank 24 after air cooler 23 is cooled to 42 DEG C, separates in flash tank 24, the top of flash tank 24 row
The mainly uncooled hydrogen put, is incorporated in synthesis gas intake pipeline 4 with the carbon monoxide allocated into, and the first carbonyl is delivered to together
In base synthesis reactor 1.
Finally, the material of the bottom of flash tank 24 discharge after drying, is delivered to depropanizing tower 26, and the top of depropanizing tower 26 can
The propylene that purity is 99.57% is obtained, is incorporated in propylene intake pipeline 3 by pipeline, the first carbonylation synthesis are delivered to together anti-
Answer in device 1, in propane reflux to the shell side of heat exchanger 17 of the bottom discharge of depropanizing tower 26, be circulated recycling.
Consumption of raw materials during propenecarbonyl can effectively be reduced using this method, one ton of butyraldehyde is often produced, propylene disappears
Consumption can reduce 6.2KG, and synthesis gas consumption can reduce 13NM3。
Although being described to function of the invention and the course of work above in conjunction with accompanying drawing, the invention is not limited in
Above-mentioned concrete function and the course of work, above-mentioned specific embodiment are only schematical, rather than restricted, ability
The those of ordinary skill in domain is not departing from present inventive concept and scope of the claimed protection situation under enlightenment of the invention
Under, many forms can also be made, these are belonged within protection of the invention.
Claims (2)
1. a kind of device for reducing consumption of raw materials during propenecarbonyl, including the first carbongl group synthesis reaction being sequentially connected
Device, the second carbonyl synthesis reactor and high pressure evaporator collecting tank, first carbonyl synthesis reactor are connected with propylene input
Pipeline and synthesis gas intake pipeline, the second carbonyl synthesis reactor top are connected with heat exchanger, it is characterised in that described to change
Gas delivery port at the top of hot device top and high pressure evaporator collecting tank is connected by pipeline with the shell side inlet of heat exchanger
Logical, the shell-side outlet of the heat exchanger is connected with electric furnace, fixed bed reactors and the first cooler in turn by pipeline,
The outlet of first cooler is connected with the tube side import of heat exchanger, and the tube side outlet of the heat exchanger passes through pipeline
It is connected with the second cooler, compressor, air cooler and flash tank in turn, the flash drum overhead is by hydrogen delivery tube line and conjunction
It is connected into gas intake pipeline, the flash tank bottom is connected with depropanizing tower, the depropanizing tower top passes through pipeline and third
Alkene intake pipeline is connected, and the depropanizing tower bottom is connected by pipeline with the shell side import of heat exchanger.
2. it is according to claim 1 it is a kind of reduce propenecarbonyl during consumption of raw materials device, it is characterised in that institute
State hydrogen delivery tube line and be communicated with carbon monoxide and allocate pipeline into.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621051799.8U CN206188684U (en) | 2016-09-13 | 2016-09-13 | Reduce device that propylene carbonylation process central plain material consumed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621051799.8U CN206188684U (en) | 2016-09-13 | 2016-09-13 | Reduce device that propylene carbonylation process central plain material consumed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206188684U true CN206188684U (en) | 2017-05-24 |
Family
ID=58728391
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621051799.8U Withdrawn - After Issue CN206188684U (en) | 2016-09-13 | 2016-09-13 | Reduce device that propylene carbonylation process central plain material consumed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206188684U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106278844A (en) * | 2016-09-13 | 2017-01-04 | 天津渤化永利化工股份有限公司 | A kind of reduce the device and method of consumption of raw materials during propenecarbonyl |
-
2016
- 2016-09-13 CN CN201621051799.8U patent/CN206188684U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106278844A (en) * | 2016-09-13 | 2017-01-04 | 天津渤化永利化工股份有限公司 | A kind of reduce the device and method of consumption of raw materials during propenecarbonyl |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101157442B (en) | Waste heat reclaiming process for CO transformation | |
| CN102850183B (en) | Methanol synthesis system and method | |
| CN104829494A (en) | Energy-saving urea production system and production process thereof | |
| CN104628589B (en) | Continuous production process and system for synthesizing N, N-dimethyl propanamide | |
| CN109748791B (en) | Energy-saving method for producing dimethyl adipate | |
| CN109400443A (en) | A kind of device and method of preparing ethylene glycol by using dimethyl oxalate plus hydrogen | |
| CN210632117U (en) | Continuous reaction device | |
| CN103896280A (en) | Operation method of polycrystalline silicon cold hydrogenation | |
| CN107011163B (en) | The method that acetylene method gas phase produces vinylacetate | |
| CN106278844A (en) | A kind of reduce the device and method of consumption of raw materials during propenecarbonyl | |
| CN106748631A (en) | A kind of monochloro methane energy-saving processing technique and device | |
| CN101058534B (en) | Device and method for preparing dimethyl ether from methanol | |
| CN206188684U (en) | Reduce device that propylene carbonylation process central plain material consumed | |
| CN109748790B (en) | Method for producing dimethyl adipate | |
| CN201596496U (en) | Cyclohexanone Ammoximation reactor | |
| CN105883852A (en) | Ammonia synthesis reaction system and method | |
| CN212102639U (en) | Device for refining cyclohexanone by cyclohexanol dehydrogenation | |
| CN108530264A (en) | New heat energy utilization system and heat energy utilization method in a kind of cyclohexanol production | |
| KR102150240B1 (en) | Alkylenecarbonate Manufacturing System and Manufacturing Method Using the Same | |
| CN209338419U (en) | A kind of cyclohexene production energy-saving system | |
| CN201775977U (en) | Treatment device for reaction tail gas in trimellitic acid production | |
| CN214456890U (en) | Tandem type double-ammonia synthesis tower | |
| CN101954198A (en) | High-pressure dehydrating tower in process of continuously producing trimellitate | |
| CN104829452B (en) | Energy-saving production system of ethyl acetate and corresponding energy-saving production technology | |
| CN103030117B (en) | Recovering technology for waste acid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20170524 Effective date of abandoning: 20200512 |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20170524 Effective date of abandoning: 20200512 |
|
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned |