CN113999195A - High-yield maleic anhydride water absorption continuous refining process - Google Patents
High-yield maleic anhydride water absorption continuous refining process Download PDFInfo
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- C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
- C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
- C07D307/34—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D307/56—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
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- 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
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Abstract
The invention discloses a high-yield maleic anhydride water absorption continuous refining process, which overcomes the defect that the existing water absorption refining process is an intermittent process. The specific technical scheme is as follows: a high-yield maleic anhydride water absorption continuous refining process comprises a crude anhydride purification and recovery section, a double-dehydration section and a crude anhydride refining section; the crude anhydride is dehydrated by a stripper, the gas phase at the top of the tower enters a water absorption tower and then is conveyed to a double-dehydration working section, and the crude anhydride at the bottom of the tower is conveyed to a crude anhydride refining working section; the double-removal section comprises a dehydration tower and a xylene removal tower, wherein the xylene removal tower adopts positive pressure operation and recovers gas phase heat at the top of the tower to the bottom of the dehydration tower; the crude anhydride refining section comprises a light component removal tower and a main fraction removal tower, wherein the bottom material of the main fraction removal tower is removed, maleic anhydride is evaporated under negative pressure, and the maleic anhydride is recycled to the bottom of the main fraction removal tower. The maleic anhydride commodity prepared by the invention has no trace impurities of solvent decomposition products, and due to the adoption of a continuous process, the dehydration energy consumption of the device is reduced, the yield of the maleic anhydride of the device is improved, the generation amount of solid wastes is reduced, and the device can be large-scale.
Description
Technical Field
The invention belongs to the field of maleic anhydride, and particularly relates to a high-yield maleic anhydride water absorption continuous refining process.
Background
Before 2013, the maleic anhydride industry takes intermittent refining after absorption of benzene oxidation water as a main part and takes intermittent refining after absorption of n-butane oxidation water as an auxiliary part. As the price of petroleum rises, the price of benzene as a raw material is far higher than that of n-butane as a raw material, the cost of an n-butane oxidation process is far lower than that of a benzene oxidation process, and after 2013, a foreign n-butane oxidation solvent (DBP) absorption process and a domestic n-butane oxidation solvent (DIBE) absorption process of a digestion and absorption foreign process are introduced, so that the process for preparing maleic anhydride by oxidizing n-butane in the maleic anhydride industry is rapidly developed, and the process for preparing maleic anhydride by oxidizing benzene is rapidly replaced. After 2013, the oxidation section of the maleic anhydride industry takes an n-butyl oxidation process as a main part and takes a benzene oxidation process as an auxiliary part; the post-treatment process mainly adopts continuous refining by organic solvent absorption and takes intermittent refining by water absorption as an auxiliary.
The existing organic solvent absorption process has the following disadvantages:
(1) in the first month when the reactor uses a new catalyst, the solvent is seriously emulsified, the solvent consumption is high, and the COD of the sewage is high;
(2) when di-n-butyl phthalate (DBP) is used as a solvent, the molecular structure of the solvent contains benzene rings, and the superior grade commodity of maleic anhydride contains a trace amount of DBP, so that the maleic anhydride produced by the process is not approved by European Union and partial users;
(3) the organic solvent is decomposed in the high-temperature environment in the absorption and analysis process, so that the final maleic anhydride high-grade commodity contains trace solvent decomposition products;
(4) the investment of the organic solvent absorption and desorption process device is large.
Meanwhile, the existing water absorption batch refining has the following defects:
(1) the content of free acid of crude anhydride separated by partial condensation reaches 3.0 percent;
(2) the dehydration refining system needs to be cleaned every 3 batches of production, and the amount of generated waste water is large;
(3) a large amount of residue is discharged after the dehydration refining kettle is cleaned, and the yield is lost by 2 percent;
(4) the American SD process package requires that the concentration of the maleic acid is controlled by 42 percent, so that the dehydration energy consumption of the device is high;
(5) the single set of equipment has a scale of less than 5 ten thousand tons/year due to the explosion hazard of the refining kettle.
Disclosure of Invention
Based on the above disadvantages, the present invention aims to provide a high yield maleic anhydride water absorption continuous refining process.
In order to achieve the purpose, the invention provides the following technical scheme:
a high-yield maleic anhydride water absorption continuous refining process comprises a crude anhydride purification and recovery section, a double-dehydration section and a crude anhydride refining section;
the crude anhydride purification and recovery section is that the reaction mixed gas is cooled to 60 ℃ and enters a cyclone separator, the separated liquid-phase crude anhydride is conveyed to a heater for heating through a pump and then enters the top of a crude anhydride gas stripping dehydration tower, the crude anhydride at the bottom of the gas stripping dehydration tower is conveyed to a crude anhydride refining section, the gas phase containing maleic anhydride separated by the cyclone separator enters the bottom of a water absorption tower, and flows into a concentrated acid water pump after being subjected to mass transfer and heat transfer with the water entering the top of the tower to generate maleic acid dissolved water and then is conveyed to a dehydration tower of a dehydration section of a double dehydration section;
in the double-dehydration section, maleic acid water from the crude anhydride purification and recovery section and dimethylbenzene refluxed from the tower top flow downwards along the tower and transfer heat with dimethylbenzene rising from the tower bottom, water in the acid water is vaporized, water vapor stripped by maleic acid and gaseous dimethylbenzene form azeotrope vapor which flows upwards along the tower, the azeotrope vapor is condensed into liquid through a tower top condenser and flows into a decanter, dimethylbenzene on the upper layer completely refluxes to the dehydration tower top, 90% of water discharged by the decanter returns to the absorption tower top to be used as absorbent, desalted water is partially supplemented when the absorbent is insufficient, sewage treatment is carried out on the other 10% of discharged water, maleic anhydride formed after the maleic acid dehydration and part of dimethylbenzene flow to the tower bottom, the maleic anhydride and part of dimethylbenzene flow into a tower bottom reboiler to provide rising gas phase for the dehydration tower, a mixture of maleic anhydride and dimethylbenzene is pumped out and sent to the top of the xylene removal tower, the liquid flows downwards to each tower tray for stepwise concentration, and the dimethylbenzene in the maleic anhydride in the tower bottom is completely evaporated, crude anhydride is extracted from the tower bottom and used as the feeding material of a crude anhydride refining section, xylene is concentrated at the tower top and returns to the bottom of a water-withdrawal tower;
in the crude anhydride refining section, crude anhydride generated in the crude anhydride purification and recovery section and crude anhydride generated at the bottom of a xylene removal tower in the double-removal section enter a light component removal tower, light components flow out of the top of the light component removal tower to a condenser at the top of the light component removal tower, extracted parts flow out of the top of the xylene removal tower, heavy components flow out of the bottom of the heavy component removal tower to a main fraction removal tower through a pump, the heavy components flow out of the bottom of the main fraction removal tower to a heavy component distillation stirring kettle, evaporated gas phase is condensed and then is pumped to the bottom of the main fraction removal tower through the pump, maleic anhydride is recovered, the light components in the main fraction removal tower are condensed through a condenser at the top of the tower, and flow back to the top of the main fraction removal tower to reflux, and are extracted to the light component removal tower to feed;
and the main fraction removing tower extracts superior maleic anhydride from a tower tray at the 14 th layer.
The gas phase at the top of the stripping dehydration tower returns to the inlet of the aftercooler or the final water inlet absorption tower; the stripping of the crude anhydride uses air or nitrogen or other gases.
The top condenser of the dehydration tower is additionally connected with a fan for exhausting, the non-condensable gas is sent out through the fan, the pressure of the dehydration tower and the pressure of the xylene removal tower are controlled, and the temperature of the bottom of the dehydration tower and the temperature of the bottom of the xylene removal tower are controlled to be less than 165 ℃.
Concentrated acid water at the bottom of the water absorption tower is directly conveyed to a dehydration tower by a pump or enters a buffer container, and the lowest liquid level is controlled to operate.
The flow of the xylene removal tower comprises a process flow of removing xylene by using a reboiler at the bottom of the tower and a condenser at the top of the tower.
And (3) feeding heavy components at the bottom of the main fraction removal tower into a stirring evaporation kettle, evaporating maleic anhydride under negative pressure, and recovering the maleic anhydride to the bottom of the main fraction removal tower or materials containing the maleic anhydride.
The refining process is characterized in that a heat exchanger system for recovering heat of materials at the top of the dehydration tower is added according to the temperature at the top of the dehydration tower, and the heat exchanger system is used for heating or is used as a reboiler of a liquefied gas separation system.
The refining process is characterized in that a heat exchanger system for recovering heat of materials at the top of the main fraction removing tower is added according to the temperature at the top of the main fraction removing tower, and the heat exchanger system is used for generating steam with the grade below 0.2 Mpa.
Compared with the prior art, the invention has the beneficial effects that:
(1) the water absorption process device of the invention has no emulsification phenomenon in the whole service life of the new catalyst.
(2) The maleic anhydride product prepared by the invention has no trace impurities of solvent decomposition products.
(3) Heating the crude anhydride generated by the cyclone separator, and then, introducing the heated crude anhydride into a stripper to remove water, so as to reduce the maleic acid content in the crude anhydride to below 0.5 percent. Solves the problems of pipeline blockage and tank blockage caused by maleic acid.
(4) The maleic anhydride yield of the device is improved by 2.5 percent due to the reduction of the maleic acid content in the crude anhydride. Greatly reduces the solid waste production of the device.
(5) The reduction of maleic acid content in the crude anhydride can prolong the operation period of the device to more than one year, and greatly reduce the amount of waste water generated by the maleic anhydride device.
(6) Because of adopting the continuous process, the residence time of the concentrated acid water is greatly reduced, the concentration of the concentrated acid water can be improved, and the dehydration energy consumption of the device is reduced.
(7) Due to the adoption of a continuous process, the residence time of the maleic anhydride in a high-temperature area is greatly reduced, the high-temperature condensation reaction of the maleic anhydride is reduced, the yield of the maleic anhydride of the device is improved, and the generation amount of solid wastes is reduced.
(8) Because of adopting the continuous refining process, the refining kettle is cancelled, the storage amount of combustible materials in the device is reduced, and the device can be enlarged in scale.
(9) The solvent purification unit is not arranged, so that the investment of the maleic anhydride water absorption continuous refining process device is low.
(10) Compared with an organic solvent absorption and analysis device, the process is simplified, the number of pumps is reduced, and the power consumption is reduced.
Drawings
FIG. 1 is a process flow diagram of the crude anhydride purification recovery section of the present invention.
FIG. 2 is a process flow diagram of the double stripping section of the present invention.
FIG. 3 is a process flow diagram of the crude anhydride refining section of the present invention.
In the figure, E310 — aftercooler; d310-cyclone separator; g310-separator bottom pump; e311-crude anhydride heater; t310-crude anhydride stripping dehydration tower; v311-crude anhydride tank; g311-crude anhydride pump; t312-absorption column; v312-concentrated sour water tank; g312-concentrated acid water pump;
e610-a reboiler at the bottom of the dehydration column; t410-a dehydration column; g410-a dehydration tower bottom pump; e411-a dehydration overhead condenser; v411-decanter; V412-Process water tank; g412-process water pump; g414-tail gas booster pump; e413-a reboiler at the bottom of the xylene removal tower; t413-a xylene removal tower; g413-a bottom pump of the xylene removal tower;
e510-a light component removal tower bottom reboiler; t510-a light component removal tower; g510-a light component removal tower bottom pump; e511-a light component removal overhead condenser; g511-a light component removal tower top reflux pump; e512-reboiler at the bottom of product refining tower; t512-main fraction removal tower; v515-raffinate tank; v514-heavy component evaporation kettle; e514-heavy component kettle top condenser; g514-pump for recovering anhydride; g513-a side draw finished product pump; g512-product tower top reflux pump; e513-product refining overhead condenser.
Detailed Description
The present invention will be described in further detail with reference to specific examples, but the embodiments of the present invention include, but are not limited to, the scope shown in the following examples.
The high-yield maleic anhydride water absorption continuous refining process of the invention is specifically described as follows.
A crude anhydride purification and recovery section:
the upstream process cools the reaction mixed gas to 135 ℃, the reaction mixed gas enters an after cooler E310 of the working section of the invention, the mixed gas is cooled to 60 ℃, the liquid-phase crude anhydride which is separated by a cyclone separator D310 is conveyed to a heater by a pump, the liquid-phase crude anhydride is heated to 140 ℃ and then enters the top of a crude anhydride stripping dehydration tower T310, the liquid-phase crude anhydride flows downwards and transfers heat with the instrument air mass transfer which rises from the bottom of the tower, and the water and the ascending gas flow which are removed from the maleic acid return to the inlet of the after cooler E310 through the gas phase at the top of the stripping tower. The crude anhydride at the bottom of the crude anhydride stripping dehydrating tower T310 enters a crude anhydride tank V311, and the crude anhydride is conveyed to a crude anhydride refining section through a pump. The outlet temperature of the aftercooler E310 is controlled by controlling the temperature and flow rate of the tempered water of the aftercooler E310.
The gas phase containing maleic anhydride from the cyclone D310 enters the bottom of a water absorption tower T312, the gas phase upwards transfers heat with water entering from the top of the tower on a tray, the maleic anhydride reacts with the water to generate maleic acid dissolved water, and then the maleic acid dissolved water flows into a concentrated acid water pump G312 and is conveyed to a dehydration tower T410 of a dehydration section. The temperature control of absorber T312 is controlled by adjusting the cooler exit temperature and the temperature of the recycled sour water that is recycled from the bottom of the water absorber to the 8 th tray above the bottom of absorber T312. The concentrated acid water tank V312 is used for storing concentrated acid water when the power-on and power-off or subsequent section faults occur (the concentrated acid water does not enter the acid water tank during normal operation). The concentration of the concentrated acid water is controlled by controlling the water supplement amount at the top of the water absorption tower.
Double stripping section:
the concentrated acid water sent to the crude anhydride purification and recovery section enters a 16 th tray of a dehydrating tower T410, flows downwards along the tower together with the dimethylbenzene refluxed from the top of the tower, conducts mass heat with the dimethylbenzene steam rising from the bottom of the tower on the tray, forms azeotropic substance steam with rising gaseous dimethylbenzene after water in the acid water is vaporized and stripped along with acid, flows upwards along the tower, is condensed into liquid through a dehydrating tower top condenser E411 and flows into a decanter V411, and is layered by gravity, and the dimethylbenzene on the upper layer totally refluxes to the top of the dehydrating tower T410. Most of the water discharged by the decanter V411 returns to the absorption tower to be used as water supplement (the recovery amount is determined according to the quality of the maleic anhydride product), and a small part of the water is treated by sewage. The maleic anhydride formed after dehydration of the maleic acid flows to the bottom of the tower, and the majority of the maleic anhydride flows into a reboiler E510 at the bottom of the dehydration tower, which provides upward flow of xylene and maleic anhydride vapor to the dehydration tower T410 and provides energy for dehydration.
The dehydration tower top condenser E411 of the dehydration tower T410 is additionally connected with a fan for exhausting, the non-condensable gas is sent out through the fan, the tower pressure of the dehydration tower T410 and the tower pressure of the xylene removal tower T413 are controlled, and the tower bottom of the dehydration tower T410 and the tower bottom of the xylene removal tower T413 are controlled to be less than 165 ℃.
And (3) pumping a mixture of maleic anhydride and xylene from the tower bottom to the top of a dimethylbenzene removal tower T413, making mass transfer and heat transfer between the mixture and the gas rising from the tower bottom in a downward flow manner, concentrating the liquid step by each tower tray, completely distilling off the xylene in the maleic anhydride from the tower bottom, and pumping crude anhydride from the tower bottom as the feeding material of a crude anhydride refining section. The xylene vapor is gradually concentrated upwards along the tower and returns to the bottom of the water-removing tower from the top of the tower, so as to supplement the xylene and energy for the dehydrating tower T410.
The top of the xylene removal tower T413 can be provided with a tower top condenser or not, wherein the tower top condenser is arranged to enable the content of maleic anhydride in a xylene stream at the top of the tower to be lower, but the energy consumption is higher, and the energy is saved without the tower top condenser.
Controlling the temperature of the top of the dehydrating tower T410 to be 98-110 ℃ through the steam quantity of a reboiler at the bottom of the dehydrating tower. The top of the dehydration column T410 is operated at atmospheric pressure. The dehydration column T410 and the xylylene removal column T413 can be understood as one column.
The xylene lost in the double-stripping section can be obtained by pumping the purchased new xylene to the top of the dehydration tower T410.
And (3) a crude anhydride refining section:
the crude anhydride generated in the crude anhydride purification and recovery section and the crude anhydride generated at the bottom of the light component removal tower T413 are sent to a lower filling section of a light component removal tower T510 in the crude anhydride refining section, flow downwards and transfer mass and heat with gas at the bottom of the tower and upwards, light components flow upwards and gradually become light, flow out of the tower top to a condenser E511 at the top of the light component removal tower, flow back to the top of the light component removal tower T510 through a reflux pump G511 at the top of the light component removal tower, and part of the light components is collected to the top of the xylene tower. Heavy components flow downwards step by step and are gradually concentrated, the heavy components are conveyed to the 6 th layer of a main fraction removal tower T512 through a pump to the bottom of the tower, the steam which flows downwards and rises with the bottom of the tower conducts mass heat on a tower tray, the heavy components are gradually concentrated to the bottom of the tower, the heavy components flowing out from the bottom of the tower are conveyed to a heavy component distillation stirring kettle to be evaporated again, the evaporated gas phase is condensed and then conveyed to the bottom of the main fraction removal tower T512 through the pump to recover maleic anhydride, residual liquid of the distillation kettle is discharged, and the cooled gas phase can be used as a raw material for producing fumaric acid, a coke raw material and fuel.
The gas phase upward along the tower is in mass transfer with the tower top reflux liquid phase on a tower tray, the ascending gas phase gradually becomes lighter, most of the liquid condensed by the tower top condenser is refluxed to the top of the main fraction removal tower T512 through a pump and is refluxed, and a small part of the liquid is extracted to the light fraction removal tower T510 to be fed (the extraction amount is controlled according to the product quality). The descending liquid is gradually purified, and the superior maleic anhydride is extracted from the tray at the 14 th layer.
Process parameters
The invention is not limited to the examples, and any equivalent changes to the technical solution of the invention by a person skilled in the art after reading the description of the invention are covered by the claims of the invention.
Claims (8)
1. A high-yield maleic anhydride water absorption continuous refining process is characterized in that:
comprises a crude anhydride purification recovery working section, a double-dehydration working section and a crude anhydride refining working section;
the crude anhydride purification and recovery section is that the reaction mixed gas is cooled to 60 ℃ and enters a cyclone separator, the separated liquid-phase crude anhydride is conveyed to a heater for heating through a pump and then enters the top of a crude anhydride gas stripping dehydration tower, the crude anhydride at the bottom of the gas stripping dehydration tower is conveyed to a crude anhydride refining section, the gas phase containing maleic anhydride separated by the cyclone separator enters the bottom of a water absorption tower, and flows into a concentrated acid water pump after being subjected to mass transfer and heat transfer with the water entering the top of the tower to generate maleic acid dissolved water and then is conveyed to a dehydration tower of a dehydration section of a double dehydration section;
in the double-dehydration section, maleic acid water from the crude anhydride purification and recovery section and dimethylbenzene refluxed from the tower top flow downwards along the tower and transfer heat with dimethylbenzene rising from the tower bottom, water in the acid water is vaporized, water vapor stripped by maleic acid and gaseous dimethylbenzene form azeotrope vapor which flows upwards along the tower, the azeotrope vapor is condensed into liquid through a tower top condenser and flows into a decanter, dimethylbenzene on the upper layer completely refluxes to the dehydration tower top, 90% of water discharged by the decanter returns to the absorption tower top to be used as absorbent, desalted water is partially supplemented when the absorbent is insufficient, sewage treatment is carried out on the other 10% of discharged water, maleic anhydride formed after the maleic acid dehydration and part of dimethylbenzene flow to the tower bottom, the maleic anhydride and part of dimethylbenzene flow into a tower bottom reboiler to provide rising gas phase for the dehydration tower, a mixture of maleic anhydride and dimethylbenzene is pumped out and sent to the top of the xylene removal tower, the liquid flows downwards to each tower tray for stepwise concentration, and the dimethylbenzene in the maleic anhydride in the tower bottom is completely evaporated, crude anhydride is extracted from the tower bottom and used as the feeding material of a crude anhydride refining section, xylene is concentrated at the tower top and returns to the bottom of a water-withdrawal tower;
in the crude anhydride refining section, crude anhydride generated in the crude anhydride purification and recovery section and crude anhydride generated at the bottom of a xylene removal tower in the double-removal section enter a light component removal tower, light components flow out of the top of the light component removal tower to a condenser at the top of the light component removal tower, extracted parts flow out of the top of the xylene removal tower, heavy components flow out of the bottom of the heavy component removal tower to a main fraction removal tower through a pump, the heavy components flow out of the bottom of the main fraction removal tower to a heavy component distillation stirring kettle, evaporated gas phase is condensed and then is pumped to the bottom of the main fraction removal tower through the pump, maleic anhydride is recovered, the light components in the main fraction removal tower are condensed through a condenser at the top of the tower, and flow back to the top of the main fraction removal tower to reflux, and are extracted to the light component removal tower to feed;
and the main fraction removing tower extracts superior maleic anhydride from a tower tray at the 14 th layer.
2. The high-yield maleic anhydride water absorption continuous refining process as claimed in claim 1, wherein:
the gas phase at the top of the stripping dehydration tower returns to the inlet of the aftercooler or the final water inlet absorption tower; the stripping of the crude anhydride uses air or nitrogen or other gases.
3. The high-yield maleic anhydride water absorption continuous refining process as claimed in claim 2, wherein:
the top condenser of the dehydration tower is additionally connected with a fan for exhausting, the non-condensable gas is sent out through the fan, the pressure of the dehydration tower and the pressure of the xylene removal tower are controlled, and the temperature of the bottom of the dehydration tower and the temperature of the bottom of the xylene removal tower are controlled to be less than 165 ℃.
4. The high-yield maleic anhydride water absorption continuous refining process as claimed in claim 3, wherein:
concentrated acid water at the bottom of the water absorption tower is directly conveyed to a dehydration tower by a pump or enters a buffer container, and the lowest liquid level is controlled to operate.
5. The high-yield maleic anhydride water absorption continuous refining process as claimed in claim 4, wherein:
the flow of the xylene removal tower comprises a process flow of removing xylene by using a reboiler at the bottom of the tower and a condenser at the top of the tower.
6. The high-yield maleic anhydride water absorption continuous refining process as claimed in claim 5, wherein:
and (3) feeding heavy components at the bottom of the main fraction removal tower into a stirring evaporation kettle, evaporating maleic anhydride under negative pressure, and recovering the maleic anhydride to the bottom of the main fraction removal tower or materials containing the maleic anhydride.
7. The high-yield maleic anhydride water absorption continuous refining process as claimed in claim 6, wherein:
the refining process is characterized in that a heat exchanger system for recovering heat of materials at the top of the dehydration tower is added according to the temperature at the top of the dehydration tower, and the heat exchanger system is used for heating or is used as a reboiler of a liquefied gas separation system.
8. The high-yield maleic anhydride water absorption continuous refining process as claimed in claim 7, wherein:
the refining process is characterized in that a heat exchanger system for recovering heat of materials at the top of the main fraction removing tower is added according to the temperature at the top of the main fraction removing tower, and the heat exchanger system is used for generating steam with the grade below 0.2 Mpa.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101157673A (en) * | 2007-11-13 | 2008-04-09 | 山西新和太明化工有限公司 | Maleic anhydride production technique |
| CN103058964A (en) * | 2013-01-25 | 2013-04-24 | 山东元利科技股份有限公司 | Method for preparing maleic anhydride by continuous dehydration method |
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2021
- 2021-11-26 CN CN202111416964.0A patent/CN113999195A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101157673A (en) * | 2007-11-13 | 2008-04-09 | 山西新和太明化工有限公司 | Maleic anhydride production technique |
| CN103058964A (en) * | 2013-01-25 | 2013-04-24 | 山东元利科技股份有限公司 | Method for preparing maleic anhydride by continuous dehydration method |
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| 何仕明等: ""苯氧化法制顺酐连续化生产工艺设计及评价"", 《化学工程》, vol. 50, no. 4, pages 73 - 78 * |
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