CN111039775A - Acetic acid synthesis catalyst separation recovery unit - Google Patents
Acetic acid synthesis catalyst separation recovery unit Download PDFInfo
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- CN111039775A CN111039775A CN201811183664.0A CN201811183664A CN111039775A CN 111039775 A CN111039775 A CN 111039775A CN 201811183664 A CN201811183664 A CN 201811183664A CN 111039775 A CN111039775 A CN 111039775A
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- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 title claims abstract description 132
- 238000000926 separation method Methods 0.000 title claims abstract description 61
- 239000003054 catalyst Substances 0.000 title claims abstract description 34
- 238000011084 recovery Methods 0.000 title claims abstract description 16
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 11
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 11
- 238000001816 cooling Methods 0.000 claims abstract description 38
- 239000012071 phase Substances 0.000 claims description 106
- 239000007791 liquid phase Substances 0.000 claims description 27
- 239000007788 liquid Substances 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 239000000463 material Substances 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 238000010521 absorption reaction Methods 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 4
- INQOMBQAUSQDDS-UHFFFAOYSA-N iodomethane Chemical compound IC INQOMBQAUSQDDS-UHFFFAOYSA-N 0.000 abstract description 16
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 abstract description 11
- 229910052703 rhodium Inorganic materials 0.000 abstract description 10
- 239000010948 rhodium Substances 0.000 abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 238000005192 partition Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 50
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 33
- 238000000034 method Methods 0.000 description 9
- XMBWDFGMSWQBCA-UHFFFAOYSA-N hydrogen iodide Chemical compound I XMBWDFGMSWQBCA-UHFFFAOYSA-N 0.000 description 7
- 229910000043 hydrogen iodide Inorganic materials 0.000 description 7
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 6
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 6
- 230000006315 carbonylation Effects 0.000 description 6
- 238000005810 carbonylation reaction Methods 0.000 description 6
- 238000004064 recycling Methods 0.000 description 6
- 239000002253 acid Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 125000004122 cyclic group Chemical group 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 238000005191 phase separation Methods 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 235000019260 propionic acid Nutrition 0.000 description 1
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 description 1
- 239000012429 reaction media Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
- C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provides an acetic acid synthesis catalyst separation recovery unit, includes pre-separator, cooler, first separator, strip tower, reboiler, lightness-removing tower, first cold cooling ware, final cooling cooler, second separator, delayer. According to the invention, through modularization and function partition design, the step-by-step efficient separation of expensive rhodium catalyst, catalyst promoter methyl iodide and crude acetic acid is realized, the unit product consumption and cost are effectively reduced, and the clean and environment-friendly index and economic benefit of the acetic acid production process are improved.
Description
Technical Field
The invention belongs to the technical field of separation, and particularly relates to a separation and recovery device for an acetic acid synthesis catalyst.
Technical Field
Among the currently used processes for the synthesis of acetic acid, the most commercially effective is the process for the production of acetic acid by the carbonylation of methanol in the presence of a rhodium catalyst comprising rhodium dissolved or dispersed in a liquid reaction medium or supported on an inert solid, a halogen-containing promoter (e.g. methyl iodide) and methyl acetate.
The traditional catalyst and light component separation and recovery system can separate and recover methyl iodide in the rhodium catalyst, and simultaneously separate and recover part of water in the form of dilute acetic acid. Compared with acetic acid (normal boiling point is 117.7 ℃), methyl acetate, methanol and water are light components, propionic acid is a heavy component, and hydrogen iodide can be ionized in water, so that the volatility of the hydrogen iodide is related to the water content, and the volatility of the hydrogen iodide is different by several orders of magnitude in 96-99% acetic acid aqueous solution.
The separation and recovery system comprises a light component removal tower, a primary cooling cooler, a final cooling cooler, a condensate separator and a layering device, wherein a small amount of rhodium catalyst is entrained in a gas phase sent to the light component removal tower from an evaporator in the process of manufacturing acetic acid by methanol carbonylation, and the gas phase is washed by a tower plate at the lower part of the light component removal tower and sent back to the evaporator from a tower kettle of the light component removal tower and then returned to a reaction kettle. The sorting, separating and recycling effect of the separation and recycling system is poor, the rhodium part of the main catalyst is moved to other systems, cannot be recycled, and the consumption is high. The primary recovery rate of the catalyst promoter methyl iodide is only 87 percent, and a large and complicated absorption system is required to be equipped for further recovering the catalyst promoter. The whole process has the disadvantages of multiple steps, complex process, high energy consumption, large equipment investment and poor economical efficiency.
Disclosure of Invention
The invention aims to provide a separation and recovery device for acetic acid synthesis catalyst, which is easy to operate, low in cost and good in separation effect, and improves the clean and environment-friendly indexes and economic benefits of the acetic acid production process.
In order to achieve the purpose, the invention provides the technical scheme that:
a separation and recovery device for acetic acid synthesis catalyst comprises:
the top end and the bottom of the pre-separation tower are respectively provided with a gas phase outlet and a liquid phase outlet, and the lower part of the pre-separation tower is provided with a gas phase inlet; the circulating liquid inlet is arranged and is higher than the gas phase inlet; a circulating pump is arranged outside the pre-separation tower, and two ends of the circulating pump are respectively connected with the bottom of the pre-separation tower and a circulating liquid inlet of the pre-separation tower;
the inlet of the cooler is connected with the gas phase outlet of the pre-separation tower through a pipeline;
the first separator is provided with a feed inlet, and the top end and the bottom end of the first separator are respectively provided with a gas phase outlet and a liquid phase outlet; the feed inlet of the first separator is connected with the outlet of the cooler through a pipeline;
the stripping tower is provided with a liquid phase inlet and a heavy phase inlet at the upper part, a reboiled liquid inlet at the lower part, and a gas phase outlet and a crude acetic acid outlet at the top end and the bottom part; a liquid phase inlet of the stripping tower is connected with a liquid phase outlet of the first separator through a pipeline;
the two ends of the reboiler are respectively connected with the bottom of the stripping tower and the reboiling liquid inlet of the stripping tower;
the top end and the bottom of the light component removal tower are respectively provided with a light phase outlet and a heavy phase outlet, and the light component removal tower is also provided with a first gas phase inlet, a second gas phase inlet and a light phase inlet, wherein the second gas phase inlet is lower than the first gas phase inlet; the first gas phase inlet of the light component removal tower is connected with the gas phase outlet of the first separator through a pipeline; the second gas phase inlet of the light component removal tower is connected with the gas phase outlet of the stripping tower through a pipeline;
the primary cooling cooler and the final cooling cooler are respectively provided with a material inlet, a condensate outlet and a non-condensable gas outlet, the material inlet of the primary cooling cooler is connected with the light phase outlet of the light component removal tower through a pipeline, and the non-condensable gas outlet of the primary cooling cooler is connected with the material inlet of the final cooling cooler through a pipeline; the non-condensable gas outlet of the final cooling cooler is communicated with a low-pressure absorption tower through a pipeline;
the second separator is provided with a condensate inlet, a material outlet and a non-condensable gas outlet; the condensate inlet of the second separator is connected with the condensate outlet of the final cooling cooler through a pipeline; the non-condensable gas outlet of the second separator is communicated with a low-pressure absorption tower through a pipeline;
the demixer is provided with a condensate inlet, a liquid phase inlet, a desalted water inlet, a light phase outlet and a heavy phase outlet; the condensate inlet of the delaminating device is connected with the condensate outlet of the primary cooling cooler through a pipeline; the liquid phase inlet of the delayer is connected with the material outlet of the second separator through a pipeline, and the desalted water inlet of the delayer is communicated with a desalted water source through a pipeline; the heavy phase outlet of the layering device is connected with the reaction kettle through a pipeline and a heavy phase pump; the light phase outlet of the delaminator is divided into two paths, one path is connected with the light phase inlet of the light component removing tower through a pipeline and a reflux pump, and the other path is connected with the reaction kettle through a pipeline and a dilute acetic acid removing pump.
Further, the liquid phase inlet and the desalted water inlet of the delaminator share one inlet through a common pipeline.
The gas phase inlet of the pre-separation tower is communicated with an evaporator in the process of manufacturing acetic acid by methanol carbonylation through a pipeline, a small amount of rhodium catalyst is clamped in the gas phase sent to the pre-separation tower from the evaporator, circulating mother liquor is provided by an external circulating pump of the pre-separation tower to be washed with a tower plate at the lower part of the pre-separation tower, the water content in the acetic acid is kept to be more than 5 percent by the kettle liquid of the pre-separation tower, most of hydrogen iodide is also left in the tower kettle, and then the hydrogen iodide is pumped back to the evaporator. The material at the top of the tower of the pre-separator discharged from the gas phase outlet of the pre-separator enters a cooler for cooling, and the gas-liquid two phases obtained by cooling are sent to a first separator for gas-liquid two-phase separation. And the gas phase separated by the first separator enters a light component removal tower for secondary separation, the separated light phase sequentially enters a primary cooling cooler and a final cooling cooler from the top end, and methyl iodide, methyl acetate, methanol and the like in the light phase are condensed, wherein the density of the methyl iodide in the condensed liquid is high (20 ℃, 2.279g/ml) and the methyl iodide is insoluble in water, so that the methyl iodide in the condensed liquid is precipitated in a delayer to form a heavy phase after entering the delayer, and the heavy phase returns to a reaction kettle in the process of preparing the acetic acid by methanol carbonylation through a heavy phase pump for recycling. Acetic acid, water, a small amount of methyl acetate and methanol in the primary cooling condenser and the final cooling cooler become light phases, one part of the light phases flows back to the light component removing tower and the stripping tower, and most of the light phases return to the reaction kettle through a dilute acid pump for recycling.
The liquid phase separated by the first separator enters a stripping tower, separation and concentration of an acetic acid product are completed in the stripping tower by means of a high-efficiency tower tray, and crude acetic acid with the concentration of about 90% is taken out from the lower part of the stripping tower and sent to a dehydrating tower.
The pre-separation tower module in the acetic acid synthesis catalyst separation and recovery device provided by the invention is provided with the circulating pump, so that the high-efficiency recovery and cyclic utilization of the noble metal catalyst are realized; the light component removal tower module design realizes effective separation of catalyst promoter methyl iodide and other light phases, and the primary recovery efficiency reaches 98 percent, thereby realizing high-efficiency recovery and cyclic utilization of the noble metal catalyst. The gas phase separated by the pre-separation tower is cooled in stages (a first-stage cooler, a second-stage primary cooler and a final cooler), so that the ordered separation of materials and the special requirements of towers with different functions on reflux liquid components are realized. The light component removal tower is connected with the stripping tower in series, the gas phase and the liquid phase are communicated with each other, the two towers share one reboiler for heat supply, the functions of crude acid concentration and light component separation are realized, and the purpose of sectional feeding and fractional separation is achieved.
The invention has the beneficial effects that:
the invention realizes the efficient separation of expensive rhodium catalyst, catalyst promoter methyl iodide and crude acetic acid step by step through modularization and function partition design, and effectively reduces the consumption and cost of unit product.
The catalyst separation and recovery device provided by the invention realizes the step-by-step efficient separation of expensive rhodium catalyst, catalyst promoter methyl iodide and crude acetic acid, reduces the consumption of the main catalyst and the catalyst promoter, simultaneously the concentration of the crude acetic acid extracted by the stripping tower is about 90%, further improves the concentration of the feed acetic acid of the dehydrating tower, reduces the energy consumption of a subsequent separation device, greatly reduces the production cost, improves the market competitiveness of acetic acid products, is easy to operate, has low cost, and obviously improves the separation effect.
Drawings
FIG. 1 is a schematic diagram of the structure of an embodiment of the present invention.
Detailed Description
The pipeline steel for very low temperature and the manufacturing method thereof according to the present invention will be further explained and explained with reference to the drawings and the specific examples, which are not to be construed as unduly limiting the technical solution of the present invention.
Example 1
Referring to fig. 1, the invention provides a separation and recovery device for acetic acid synthesis catalyst, which comprises,
the top end and the bottom of the pre-separation tower 1 are respectively provided with a gas phase outlet 101 and a liquid phase outlet 102, and the lower part of the pre-separation tower is provided with a gas phase inlet 103; a circulating liquid inlet 104 is further arranged, and the position of the circulating liquid inlet 104 is higher than that of the gas phase inlet 103; a circulating pump 2 is arranged outside the pre-separation tower 1, and two ends of the circulating pump 2 are respectively connected with the bottom of the pre-separation tower 1 and a circulating liquid inlet 104 of the pre-separation tower 1;
a cooler 3, the inlet of which is connected with the gas phase outlet 101 of the pre-separation tower 1 through a pipeline;
the first separator 4 is provided with a feed inlet 401, and the top end and the bottom end of the first separator are respectively provided with a gas phase outlet 402 and a liquid phase outlet 403; the feed port 401 of the first separator 4 is connected with the outlet of the cooler 3 through a pipeline;
a stripping tower 5, the upper part of which is provided with a liquid phase inlet 501 and a heavy phase inlet 502 respectively, the lower part of which is provided with a reboiled liquid inlet 503, and the top end and the bottom of which are provided with a gas phase outlet 504 and a crude acetic acid outlet 505 respectively; a liquid phase inlet 501 of the stripping column 5 is connected with the liquid phase outlet 403 of the first separator 4 through a pipeline;
a reboiler 6, both ends of which are respectively connected with the bottom of the stripping tower 5 and a reboiling liquid inlet 503 of the stripping tower 5;
a light phase outlet 701 and a heavy phase outlet 702 are respectively arranged at the top end and the bottom of the light component removal tower 7, a first gas phase inlet 703, a second gas phase inlet 704 and a light phase inlet 705 are also arranged on the light component removal tower, and the position of the second gas phase inlet 704 is lower than that of the first gas phase inlet 703; the first gas phase inlet 703 of the light component removal tower 7 is connected with the gas phase outlet 402 of the first separator 4 through a pipeline; a second gas phase inlet 704 of the light component removal tower 7 is connected with the gas phase outlet 504 of the stripping tower 5 through a pipeline;
the primary cooling cooler 8 and the final cooling cooler 9 are respectively provided with a material inlet 801/901, a condensate outlet 802/902 and a non-condensable gas outlet 803/903, the material inlet 801 of the primary cooling cooler 8 is connected with the light phase outlet 701 of the light component removal tower 7 through a pipeline, and the non-condensable gas outlet 803 of the primary cooling cooler 8 is connected with the material inlet 901 of the final cooling cooler 9 through a pipeline; a non-condensable gas outlet 903 of the final cooling cooler 9 is communicated with a low-pressure absorption tower A through a pipeline;
the second separator 10 is provided with a condensate inlet 1001, a material outlet 1002 and a noncondensable gas outlet 1003; the condensate inlet 1001 of the second separator 10 is connected to the condensate outlet 902 of the final cooler 9 by a pipe; a non-condensable gas outlet 1003 of the second separator 10 is communicated with the low-pressure absorption tower A through a pipeline;
the delayer 11 is provided with a condensate inlet 1101, a liquid phase inlet 1102, a desalted water inlet 1103, a light phase outlet 1104 and a heavy phase outlet 1105 respectively; the condensate inlet 1101 of the delaminator 11 is connected with the condensate outlet 802 of the primary cooler 8 through a pipeline; the liquid phase inlet 1102 of the delaminator 11 is connected with the material outlet 1002 of the second separator 10 through a pipeline, and the desalted water inlet 1103 of the delaminator 11 is communicated with a desalted water source through a pipeline; the heavy phase outlet 1105 of the delaminator 11 is connected with the reaction kettle B through a pipeline and a heavy phase pump 12; the light phase outlet 1104 of the layering device 11 is divided into two paths, one path is connected with the light phase inlet 705 of the light component removal tower 7 through a pipeline and a reflux pump 13, and the other path is connected with the reaction kettle B through a pipeline and a pump 14.
Further, the liquid phase inlet 1102 and the desalted water inlet 1103 of the delaminator 11 share an inlet through a common pipe.
In the embodiment, a gas phase inlet 103 of a pre-separation tower 1 is communicated with an evaporator C in the process of manufacturing acetic acid by methanol carbonylation through a pipeline, a small amount of rhodium catalyst is clamped in a gas phase sent to the pre-separation tower 1 from the evaporator C, a circulating mother liquor is provided by an external circulating pump 2 of the pre-separation tower 1 to be washed with a tower plate at the lower part of the pre-separation tower 1, the water content of acetic acid in a kettle of the pre-separation tower is kept to be more than 5%, most of hydrogen iodide is also left in the kettle, and then the hydrogen iodide is pumped back to the evaporator C. The material at the top of the pre-separator tower discharged from the gas phase outlet 101 of the pre-separation tower 1 enters a cooler 3 for cooling, and the gas-liquid two phases obtained by cooling are sent to a first separator 4 for gas-liquid two-phase separation. The gas phase separated by the first separator 4 enters a light component removal tower 7 for secondary separation, the separated light phase sequentially enters a primary cooling cooler 8 and a final cooling cooler 9 from the top end, and methyl iodide, methyl acetate, methanol and the like in the light phase are condensed, wherein the density of the methyl iodide in the condensed liquid is high (20 ℃, 2.279g/ml) and the methyl iodide is insoluble in water, so the methyl iodide enters a delayer 11 and is precipitated in the delayer 11 to form a heavy phase, and the heavy phase returns to a reaction kettle A in the process of preparing acetic acid by methanol carbonylation through a heavy phase pump 12 for recycling. Acetic acid, water, a small amount of methyl acetate and methanol in the primary cooling condenser 8 and the final cooling cooler 9 become light phases, one part of the light phases flows back to the light component removing tower 7 and the stripping tower 5, and most of the light phases return to the reaction kettle B through a dilute acid pump for recycling.
The liquid phase separated by the first separator 4 enters a stripping tower 5, separation and concentration of an acetic acid product are completed in the stripping tower 5 by means of a high-efficiency tower tray, and crude acetic acid with the concentration of about 90% is taken out from the lower part of the stripping tower 5 and sent to a dehydrating tower D.
According to the invention, through the modularized and function-partitioned design, the step-by-step efficient separation of expensive rhodium catalyst, catalyst promoter methyl iodide and crude acetic acid is realized, the consumption of the main catalyst promoter is reduced, the concentration of the feed acetic acid of the dehydration tower is further improved, the energy consumption of a subsequent separation device is reduced, the production cost is greatly reduced, and the market competitiveness of acetic acid products is improved.
Claims (2)
1. A separation and recovery device for acetic acid synthesis catalyst is characterized in that the device comprises,
the top end and the bottom of the pre-separation tower are respectively provided with a gas phase outlet and a liquid phase outlet, and the lower part of the pre-separation tower is provided with a gas phase inlet; a circulating liquid inlet is also arranged, and the position of the circulating liquid inlet is higher than that of the gas phase inlet; a circulating pump is arranged outside the pre-separation tower, and two ends of the circulating pump are respectively connected with the bottom of the pre-separation tower and a circulating liquid inlet of the pre-separation tower;
the inlet of the cooler is connected with the gas phase outlet of the pre-separation tower through a pipeline;
the first separator is provided with a feed inlet, and the top end and the bottom end of the first separator are respectively provided with a gas phase outlet and a liquid phase outlet; the feed inlet of the first separator is connected with the outlet of the cooler through a pipeline;
the stripping tower is provided with a liquid phase inlet and a heavy phase inlet at the upper part, a reboiled liquid inlet at the lower part, and a gas phase outlet and a crude acetic acid outlet at the top end and the bottom part; a liquid phase inlet of the stripping tower is connected with a liquid phase outlet of the first separator through a pipeline;
the two ends of the reboiler are respectively connected with the bottom of the stripping tower and the reboiling liquid inlet of the stripping tower;
the top end and the bottom of the light component removal tower are respectively provided with a light phase outlet and a heavy phase outlet, and the light component removal tower is also provided with a first gas phase inlet, a second gas phase inlet and a light phase inlet, wherein the second gas phase inlet is lower than the first gas phase inlet; the first gas phase inlet of the light component removal tower is connected with the gas phase outlet of the first separator through a pipeline; the second gas phase inlet of the light component removal tower is connected with the gas phase outlet of the stripping tower through a pipeline;
the primary cooling cooler and the final cooling cooler are respectively provided with a material inlet, a condensate outlet and a non-condensable gas outlet, the material inlet of the primary cooling cooler is connected with the light phase outlet of the light component removal tower through a pipeline, and the non-condensable gas outlet of the primary cooling cooler is connected with the material inlet of the final cooling cooler through a pipeline; the non-condensable gas outlet of the final cooling cooler is communicated with a low-pressure absorption tower through a pipeline;
the second separator is provided with a condensate inlet, a material outlet and a non-condensable gas outlet; the condensate inlet of the second separator is connected with the condensate outlet of the final cooling cooler through a pipeline; the non-condensable gas outlet of the second separator is communicated with a low-pressure absorption tower through a pipeline;
the demixer is provided with a condensate inlet, a liquid phase inlet, a desalted water inlet, a light phase outlet and a heavy phase outlet; the condensate inlet of the delaminating device is connected with the condensate outlet of the primary cooling cooler through a pipeline; the liquid phase inlet of the delayer is connected with the material outlet of the second separator through a pipeline, and the desalted water inlet of the delayer is communicated with a desalted water source through a pipeline; the heavy phase outlet of the layering device is connected with the reaction kettle through a pipeline and a heavy phase pump; the light phase outlet of the delaminator is divided into two paths, one path is connected with the light phase inlet of the light component removing tower through a pipeline and a reflux pump, and the other path is connected with the reaction kettle through a pipeline and a dilute acetic acid removing pump.
2. The apparatus for separating and recovering the catalyst used in the synthesis of acetic acid according to claim 1, wherein the inlet for the liquid phase of the layering device and the inlet for the desalted water share a common inlet through a common pipe.
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Citations (4)
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|---|---|---|---|---|
| CN1944373A (en) * | 2006-08-10 | 2007-04-11 | 上海吴泾化工有限公司 | Improved acetic acid purifying device |
| US20090088587A1 (en) * | 2007-09-27 | 2009-04-02 | Nathan Kirk Powell | Method and apparatus for making acetic acid with improved purification |
| CN101665424A (en) * | 2009-07-16 | 2010-03-10 | 北京泽华化学工程有限公司 | Method for synthesizing acetic acid through low-pressure methanol carbonylation and device thereof |
| CN208995418U (en) * | 2018-10-11 | 2019-06-18 | 河南顺达新能源科技有限公司 | A kind of acetic synthesis separation and recovery of catalyst device |
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2018
- 2018-10-11 CN CN201811183664.0A patent/CN111039775B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1944373A (en) * | 2006-08-10 | 2007-04-11 | 上海吴泾化工有限公司 | Improved acetic acid purifying device |
| US20090088587A1 (en) * | 2007-09-27 | 2009-04-02 | Nathan Kirk Powell | Method and apparatus for making acetic acid with improved purification |
| CN101665424A (en) * | 2009-07-16 | 2010-03-10 | 北京泽华化学工程有限公司 | Method for synthesizing acetic acid through low-pressure methanol carbonylation and device thereof |
| CN208995418U (en) * | 2018-10-11 | 2019-06-18 | 河南顺达新能源科技有限公司 | A kind of acetic synthesis separation and recovery of catalyst device |
Non-Patent Citations (1)
| Title |
|---|
| 谢润兴;颜庭政;唐红萍;: "甲醇低压羰基合成醋酸工艺、流程及控制新进展", 精细化工原料及中间体, no. 12, pages 6 - 12 * |
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