CN115193360A - Method and system for producing electronic isopropanol by propylene hydration method - Google Patents
Method and system for producing electronic isopropanol by propylene hydration method Download PDFInfo
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- CN115193360A CN115193360A CN202210931658.9A CN202210931658A CN115193360A CN 115193360 A CN115193360 A CN 115193360A CN 202210931658 A CN202210931658 A CN 202210931658A CN 115193360 A CN115193360 A CN 115193360A
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- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 title claims abstract description 288
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 92
- 230000036571 hydration Effects 0.000 title claims abstract description 57
- 238000006703 hydration reaction Methods 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000002994 raw material Substances 0.000 claims abstract description 23
- 230000007246 mechanism Effects 0.000 claims abstract description 20
- 238000007670 refining Methods 0.000 claims abstract description 9
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 100
- 239000007788 liquid Substances 0.000 claims description 70
- 238000000605 extraction Methods 0.000 claims description 42
- 238000000926 separation method Methods 0.000 claims description 20
- 230000018044 dehydration Effects 0.000 claims description 19
- 238000006297 dehydration reaction Methods 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 239000000203 mixture Substances 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 claims description 10
- 238000002156 mixing Methods 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 7
- 239000000243 solution Substances 0.000 claims description 6
- 239000002912 waste gas Substances 0.000 claims description 6
- 125000004122 cyclic group Chemical group 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 3
- 239000000376 reactant Substances 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims description 3
- 230000005484 gravity Effects 0.000 abstract description 3
- 238000002360 preparation method Methods 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 9
- 230000008569 process Effects 0.000 description 8
- 230000009471 action Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000010574 gas phase reaction Methods 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/002—Avoiding undesirable reactions or side-effects, e.g. avoiding explosions, or improving the yield by suppressing side-reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/40—Extractive distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
- B01D3/4227—Head- and bottom stream
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/86—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by liquid-liquid treatment
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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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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Abstract
The invention discloses a method and a system for producing electronic isopropanol by a propylene hydration method, and relates to the technical field of isopropanol preparation. The device comprises a rough mechanism and a refining mechanism, wherein the rough mechanism comprises a propylene feeding buffer tank, a water feeding buffer tank, a first delivery pump connected to the propylene feeding buffer tank, a second delivery pump connected to the water feeding buffer tank, a water feeding rough mixer connected to the second delivery pump, a raw material mixer connected to the water feeding rough mixer, a heat exchanger connected to the raw material mixer, a first heater connected to the heat exchanger, a first propylene hydration reactor connected to the first heater, a second propylene hydration reactor connected to the first propylene hydration reactor, and a second heater connected to the heat exchanger. The invention not only optimizes the specific gravity of the required extractant and the isopropanol product, but also can improve the total yield of the isopropanol product.
Description
Technical Field
The invention relates to the technical field of isopropanol preparation, in particular to a method and a system for producing electronic isopropanol by a propylene hydration method
Background
In the isopropanol production process, the method for generating isopropanol by water and isopropanol by propylene under the action of a catalyst has the characteristics of high yield and simple operation. The direct hydration method includes three methods of gas phase (weiba method), liquid phase (solution exchange method) and gas-liquid mixing (ion exchange resin method). The Viba process is currently one of the major processes for the production of isopropanol.
Since the weiba process is a gas phase reaction, water needs to be converted into a gas state in order to prevent phosphoric acid from being separated out, so that high-temperature and low-pressure reaction conditions which are unfavorable for chemical equilibrium are adopted, the conversion rate of propylene is greatly reduced, a large amount of unreacted propylene needs to be recycled repeatedly, and the cyclic processes of evaporation, condensation and the like of water exist in the process, so that the energy consumption is increased. The existing propylene gas phase direct hydration methods have similar problems, which cause the traditional isopropanol production process to have smaller profit margin and more energy consumption, so that the traditional production process needs to be reformed urgently, new requirements on indexes such as energy consumption, water consumption, carbon emission and the like are provided along with the departure of 2025 made by China, and the upgrading and the reconstruction of the traditional process are particularly important.
Disclosure of Invention
The invention aims to provide a method and a system for producing electronic isopropanol by a propylene hydration method, which are used for optimizing the specific gravity of a required extracting agent and a product and improving the total yield of the product isopropanol.
In order to achieve the purpose, the invention provides the following technical scheme: a system for producing electronic isopropanol by a propylene hydration method comprises a rough mechanism and a refining mechanism, wherein the rough mechanism comprises a propylene feeding buffer tank, a water feeding buffer tank, a first delivery pump connected to the propylene feeding buffer tank, a second delivery pump connected to the water feeding buffer tank, a water feeding rough mixer connected to the second delivery pump, a raw material mixer connected to the water feeding rough mixer, a heat exchanger connected to the raw material mixer, a first heater connected to the heat exchanger, a first propylene hydration reactor connected to the first heater, a second propylene hydration reactor connected to the first propylene hydration reactor, a second heater connected to the heat exchanger, a crude isopropanol gas-liquid separator connected to the second heater, a crude isopropanol gas-liquid separator connected to the crude isopropanol gas-liquid separator, a crude isopropanol rectifying tower connected to the crude isopropanol gas-liquid separator, a crude propylene knockout connected to the crude isopropanol rectifying tower, a compressor connected to the crude propylene knockout tower, a crude isopropanol mixer connected to the crude isopropanol rectifying tower, and a third mixing heater connected to the crude isopropanol rectifying tower, the refining mechanism comprises an isopropanol rough separation tower connected with the third heater, a fourth heater connected with the isopropanol rough separation tower, an isopropanol rectification tower connected with the fourth heater, a third delivery pump connected with the isopropanol rectification tower, a fifth heater connected with the third delivery pump, an extraction tower connected with the fifth heater, an ethylene glycol feeding mixer connected with the extraction tower, a fourth delivery pump connected with the extraction tower, A sixth heater connected to the fourth delivery pump, a fifth delivery pump connected to the extraction tower, a dehydration tower connected to the fifth delivery pump, a seventh delivery pump connected to the dehydration tower, and a seventh heater connected to the seventh delivery pump.
Further, the crude isopropanol gas-liquid separator and the crude isopropanol mixer are connected with each other.
Further, the compressor is connected with the raw material mixer.
Further, the second propylene hydration reactor and the heat exchanger are connected with each other.
Furthermore, one side of the seventh heater is connected with a seventh delivery pump, and the other side of the seventh heater is connected with an ethylene glycol feeding mixer.
A production method of a system for producing electronic isopropanol by a propylene hydration method comprises the following steps:
s1: pressurizing liquid propylene in a propylene feeding buffer tank and water in a water feeding buffer tank to 2.5MPa, conveying the liquid propylene to a raw material mixer by using a first conveying pump, conveying the water to the raw material mixer by using a second conveying pump and a water feeding coarse mixer, mixing the water and the liquid propylene, performing heat exchange on the mixture by using a heat exchanger, heating the mixture of the water and the liquid propylene to 171 ℃ by using a first heater, and sequentially allowing the mixture to enter a first propylene hydration reactor and a second propylene hydration reactor for reaction;
s2, after reacting liquid propylene with water, generating a heat flow strand consisting of isopropanol and other side reactants, reducing the temperature of the heat flow strand flowing out of a second propylene hydration reactor to 70 ℃ after the heat exchanger and a second heater act on the heat flow strand, then enabling the heat flow strand to enter a gas-liquid separator for gas-liquid separation operation, forming a gas stream and a liquid stream after separation, enabling the formed gas stream to enter a crude isopropanol rectifying tower, enabling the stream with incomplete reaction to exist at the top of the crude isopropanol rectifying tower after rectification, enabling the stream to enter a crude isopropanol knockout vessel for waste gas discharge, then utilizing a compressor to pressurize the residual stream with incomplete reaction and then reflux the residual stream to a raw material mixer for mixing and reaction again, and enabling the liquid to still distill off at the bottom of the crude isopropanol rectifying tower after rectification, and enabling the liquid and the liquid stream generated in the gas-liquid separator to flow into the crude isopropanol mixer for mixing;
s3: the mixed stream is heated by a third heater and then enters an isopropanol crude separation tower, waste gas is discharged from the top of the isopropanol crude separation tower, liquid at the bottom of the tower is heated to 105 ℃ by a fourth heater and then enters an isopropanol rectifying tower, waste liquid flows out from the bottom of the isopropanol rectifying tower, an isopropanol stream flows out from the top of the tower, the isopropanol stream is conveyed to a fifth heater by a third conveying pump to be heated, and then conveyed to an extraction tower to be extracted after being heated, meanwhile, ethylene glycol is conveyed to the extraction tower by an ethylene glycol feeding mixer, residual azeotropic water in the isopropanol stream is extracted by the ethylene glycol, and the isopropanol is separated and purified;
s4: after extraction is finished, an isopropanol product flowing out of the top of the extraction tower is pressurized to 0.7MPa through a fourth delivery pump, then delivered to a sixth heater for condensation and cooling to 30 ℃, and then enters a storage tank for storage;
s5: after extraction is finished, the bottom of the extraction tower can flow out of the ethylene glycol extraction mixed solution, the solution is pressurized to 0.7MPa by a fifth delivery pump and then is delivered to a dehydration tower, wastewater flows out of the top of the dehydration tower, the ethylene glycol at the bottom of the extraction tower is pressurized to 0.7MPa by a seventh delivery pump and then is condensed and cooled to 40 ℃ by a seventh heater, and then the ethylene glycol enters an ethylene glycol feeding mixer, so that cyclic utilization of the ethylene glycol can be realized.
Further, the operation pressure of the crude isopropanol rectifying tower is 2.2MPa, the tower top temperature is 42 ℃, and the tower kettle temperature is 145 ℃.
Further, the operating pressure of the first propylene hydration reactor was 2.3MPa, and the operating temperature was 170 ℃.
Further, the operating temperature of the second propylene hydration reactor is 210 ℃, and the operating pressure is 2.3MPa.
Further, the operating pressure of the extraction tower is 0.18MPa, the tower top temperature is 88 ℃, and the tower kettle temperature is 174 ℃.
The invention has at least the following beneficial effects:
according to the invention, through the mutual matching of the rough mechanism and the refining mechanism, liquid propylene and water can be mixed and heated and then sequentially enter the first propylene hydration reactor and the second propylene hydration reactor to react to generate isopropanol and other side reaction products, after heat flow streams from the second propylene hydration reactor are subjected to heat exchange, temperature reduction and other operations by the heat exchanger, gas-liquid separation is carried out by the gas-liquid separator, gas streams enter the top of the crude isopropanol rectification tower, and streams at the top of the tower are incomplete in reaction streams, so that the streams are pressurized and refluxed to the raw material mixer by the compressor to be mixed, a circulation reaction is facilitated, and the conversion rate is improved; the liquid distilled from the bottom of the crude isopropanol rectifying tower and the liquid separated by the gas-liquid separator are mixed and flow to the isopropanol refining section; the extraction tower absorbs the residual azeotropic water in the stream through the glycol, and the isopropanol is separated and purified; the isopropanol product with the purity of more than 99.9 percent flows out of the top of the extraction tower and enters a storage tank, the extractant mixture flows out of the bottom of the extraction tower and flows to a dehydration tower, the dehydration tower separates ethylene glycol and water, the water is distilled out of the top of the extraction tower, and the ethylene glycol is distilled out of the bottom of the extraction tower and recycled, so that the isopropanol is prepared in such a way, the specific gravity of the required extractant and the isopropanol product is optimized, and the total yield of the isopropanol product can be improved to 99 percent.
Of course, it is not necessary for any product in which the invention is practiced to achieve all of the above-described advantages at the same time.
Drawings
FIG. 1 is a schematic flow diagram of the roughing apparatus of the present invention;
FIG. 2 is a schematic flow diagram of the refining mechanism of the present invention.
Reference numerals:
100. a roughing mechanism; 1. a propylene feed surge tank; 2. a first delivery pump; 3. a water feed surge tank; 4. a second delivery pump; 5. a water feed coarse mixer; 6. a raw material mixer; 7. a heat exchanger; 8. a first heater; 9. a first propylene hydration reactor; 10. a second propylene hydration reactor; 11. a second heater; 12. a crude isopropanol gas-liquid separator; 13. a crude isopropanol rectification column; 14. a crude propylene knockout; 15. a compressor; 16. a crude isopropanol mixer; 17. a third heater;
200. a refining mechanism; 18. an isopropanol crude separation tower; 19. a fourth heater; 20. an isopropanol rectification column; 21. a third delivery pump; 22. fifth heating device; 23. a glycol feed mixer; 24. an extraction tower; 25. a fourth delivery pump; 26. a fifth delivery pump; 27. a sixth heater; 28. a dehydration tower; 29. a seventh delivery pump; 30. and a seventh heater.
Detailed Description
The technical solutions in the embodiments of the present disclosure will be clearly and completely described below with reference to the drawings in the embodiments of the present disclosure, and it is obvious that the described embodiments are only a part of the embodiments of the present disclosure, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments disclosed herein without making any creative effort, shall fall within the protection scope of the present disclosure.
Referring to fig. 1-2, the present invention provides a technical solution: a system for producing electronic isopropanol by a propylene hydration method comprises a rough mechanism 100 and a refined mechanism 200, wherein the rough mechanism 100 comprises a propylene feeding buffer tank 1 and a water feeding buffer tank 3, a first delivery pump 2 connected to the propylene feeding buffer tank 1, a second delivery pump 4 connected to the water feeding buffer tank 3, a water feeding rough mixer 5 connected to the second delivery pump 4, a raw material mixer 6 connected to the water feeding rough mixer 5, a heat exchanger 7 connected to the raw material mixer 6, a first heater 8 connected to the heat exchanger 7, a first propylene hydration reactor 9 connected to the first heater 8, the operating pressure of the first propylene hydration reactor 9 is 2.3MPa, the operating temperature is 170 ℃, a second propylene hydration reactor 10 connected to the first propylene hydration reactor 9, the operating temperature of the second propylene hydration reactor 10 is 210 ℃, the operation pressure is 2.3MPa, the second propylene hydration reactor 10 and the heat exchanger 7 are mutually connected, heat exchange and cooling of a heat flow strand flowing out of the second propylene hydration reactor 10 are conveniently carried out, the second heater 11 is connected to the heat exchanger 7, the crude isopropanol gas-liquid separator 12 is connected to the second heater 11, the crude isopropanol gas-liquid separator 12 is connected to the crude isopropanol gas-liquid separator 12, the crude isopropanol rectifying tower 13 is connected to the crude isopropanol gas-liquid separator 12, the operation pressure of the crude isopropanol rectifying tower 13 is 2.2MPa, the tower top temperature is 42 ℃, the tower bottom temperature is 145 ℃, the crude propylene knockout 14 is connected to the crude isopropanol rectifying tower 13, the compressor 15 is connected to the crude propylene knockout 14, the compressor 15 is connected to the raw material mixer 6, the residual reaction stream in the crude isopropanol knockout is conveniently pressurized and then flows back to the raw material mixer 6 for mixing again, a crude isopropanol mixer 16 connected to the crude isopropanol rectifying tower 13 for facilitating the circulation reaction, and a third heater 17 connected to the crude isopropanol mixer 16.
The refining mechanism 200 includes an isopropyl alcohol crude separation tower 18 connected to the third heater 17, a fourth heater 19 connected to the isopropyl alcohol crude separation tower 18, an isopropyl alcohol rectification tower 20 connected to the fourth heater 19, the isopropyl alcohol rectification tower 20 operates at a pressure of 0.26MPa, the tower top temperature is 128 ℃, the tower bottom temperature is 98 ℃, a third delivery pump 21 connected to the isopropyl alcohol rectification tower 20, a fifth heater 22 connected to the third delivery pump 21, and an extraction tower 24 connected to the fifth heater 22, the extraction tower 24 operates at a pressure of 0.18MPa, the tower top temperature is 88 ℃, the tower bottom temperature is 174 ℃, an ethylene glycol feed mixer 23 connected to the extraction tower 24, a fourth delivery pump 25 connected to the extraction tower 24, a sixth heater 27 connected to the fourth delivery pump 25, a fifth delivery pump 26 connected to the extraction tower 24, a dehydration tower 28 connected to the fifth delivery pump 26, the operation pressure of the dehydration tower 28 is 0.13MPa, the tower top temperature is 90 ℃, the fifth delivery pump 28 connected to the extraction tower 24, the seventh delivery pump 30 connected to the seventh delivery pump, and the dehydration tower 23 is connected to the seventh delivery pump, and the dehydration tower is connected to the seventh delivery pump, and the ethylene glycol feed mixer 23, and the dehydration tower is connected to the dehydration tower.
It should be noted that the crude isopropanol gas-liquid separator 12 and the crude isopropanol mixer 16 are connected to each other, so that the liquid separated in the gas-liquid separator can be conveniently conveyed into the crude isopropanol mixer 16.
Further, the heat exchanger 7 uses the floating head heat exchanger 7, and the tube plates at the two ends of the floating head heat exchanger 7 have one end which is not connected with the shell of the heat exchanger 7, so that when the shell and the tube bundle cause different thermal Tong expansion of different surfaces due to different temperatures, the thermal stress can be eliminated.
A production method of a system for producing electronic isopropanol by a propylene hydration method comprises the following steps:
s1: pressurizing liquid propylene in a propylene feeding buffer tank 1 and water in a water feeding buffer tank 3 to 2.5MPa, conveying the liquid propylene into a raw material mixer 6 by using a first conveying pump 2, conveying the water into the raw material mixer 6 by using a second conveying pump 4 and a water feeding coarse mixer 5, mixing the water and the liquid propylene, performing heat exchange on the mixture by using a heat exchanger 7, heating the mixture of the water and the liquid propylene to 171 ℃ by using a first heater 8, and sequentially allowing the mixture to enter a first propylene hydration reactor 9 and a second propylene hydration reactor 10 for reaction;
s2, after the liquid propylene reacts with water, a heat flow strand consisting of isopropanol and other side reactants is generated, the temperature of the heat flow strand flowing out of the second propylene hydration reactor 10 is reduced to 70 degrees after the heat exchanger 7 and the second heater 11 act, then the heat flow strand enters a gas-liquid separator to be subjected to gas-liquid separation operation, a gas flow and a liquid flow are formed after separation, the formed gas flow enters the crude isopropanol rectifying tower 13, the incompletely-reacted flow exists at the top of the crude isopropanol rectifying tower 13 after rectification, the incompletely-reacted flow enters the crude isopropanol knockout vessel to be subjected to waste gas discharge, the remaining incompletely-reacted flow is pressurized by a compressor 15 and then flows back to the raw material mixer 6 to be mixed and reacted again, liquid can be distilled off at the bottom of the crude isopropanol rectifying tower 13 after rectification, and the liquid flow generated in the gas-liquid separator into the crude isopropanol mixer 16 to be mixed;
s3: the mixed stream is heated by a third heater 17, then enters an isopropanol crude separation tower 18, waste gas is discharged from the top of the isopropanol crude separation tower 18, liquid at the bottom of the tower is heated to 105 ℃ by a fourth heater 19 and enters an isopropanol rectifying tower 20, waste liquid flows out from the bottom of the isopropanol rectifying tower 20, an isopropanol stream flows out from the top of the tower, then the isopropanol stream is conveyed into a fifth heater 22 by a third conveying pump 21 to be heated, and is conveyed into an extraction tower 24 to be extracted after being heated, meanwhile, ethylene glycol is conveyed into an extraction tower 24 by an ethylene glycol feeding mixer 23, residual azeotropic water in the isopropanol stream is extracted by the ethylene glycol, and the isopropanol is separated and purified;
s4: after extraction is finished, an isopropanol product flowing out of the top of the extraction tower 24 is pressurized to 0.7MPa through a fourth delivery pump 25, then is delivered to a sixth heater 27 to be condensed and cooled to 30 ℃, and then enters a storage tank for storage;
s5: after extraction is finished, the ethylene glycol extraction mixed solution flows out of the bottom of the extraction tower 24, the solution is pressurized to 0.7MPa by a fifth delivery pump 26 and then is delivered to a dehydration tower 28, wastewater flows out of the top of the dehydration tower 28, the ethylene glycol at the bottom of the tower is pressurized to 0.7MPa by a seventh delivery pump and then is condensed and cooled to 40 ℃ by a seventh heater 30, and then the ethylene glycol enters an ethylene glycol feeding mixer 23, so that cyclic utilization of the ethylene glycol can be realized.
The isopropyl alcohol product produced had the following composition:
the reaction conditions were: temperature: pressure at 30 ℃:0.65mpa
Molar enthalpy-75.754 kcal/mol entropy-108.049 cal/mol-K
It should be noted that, in this document, relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.
The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations. When an element is referred to as being "mounted to," "secured to," or "disposed on" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. The terms "vertical," "horizontal," "upper," "lower," "left," "right," and the like as used herein are for illustrative purposes only and do not denote a unique embodiment.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
In the description of the present specification, reference to the description of "one embodiment," "an example," "a specific example," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present disclosure. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
Claims (10)
1. A system for producing electronic isopropanol by a propylene hydration method is characterized by comprising a rough mechanism (100) and a refined mechanism (200);
the crude mechanism (100) comprises a propylene feeding buffer tank (1), a water feeding buffer tank (3), a first delivery pump (2) connected to the propylene feeding buffer tank (1), a second delivery pump (4) connected to the water feeding buffer tank (3), a water feeding crude mixer (5) connected to the second delivery pump (4), a raw material mixer (6) connected to the water feeding crude mixer (5), a heat exchanger (7) connected to the raw material mixer (6), a first heater (8) connected to the heat exchanger (7), a first propylene hydration reactor (9) connected to the first heater (8), a second propylene hydration reactor (10) connected to the first propylene hydration reactor (9), a second heater (11) connected to the heat exchanger (7), a crude isopropanol gas-liquid separator (12) connected to the second heater (11), a crude isopropanol gas-liquid separator (12) connected to the crude isopropanol gas-liquid separator (12), a crude isopropanol gas-liquid separator (13) connected to the crude isopropanol gas-liquid separator (13), a crude isopropanol liquid separator (13) connected to the crude isopropanol gas-liquid separator (13), and a crude isopropanol liquid separator (14) connected to the crude isopropanol liquid separator (13), A third heater (17) connected to the crude isopropanol mixer (16);
the refining mechanism (200) comprises an isopropanol rough separation tower (18) connected to the third heater (17), a fourth heater (19) connected to the isopropanol rough separation tower (18), an isopropanol rectification tower (20) connected to the fourth heater (19), a third conveying pump (21) connected to the isopropanol rectification tower (20), a fourth heater (22) connected to the third conveying pump (21), an extraction tower (24) connected to the fifth heater (22), an ethylene glycol feeding mixer (23) connected to the extraction tower (24), a fourth conveying pump (25) connected to the extraction tower (24), a sixth heater (27) connected to the fourth conveying pump (25), a fifth conveying pump (26) connected to the extraction tower (24), a dehydration tower (28) connected to the fifth conveying pump (26), a seventh conveying pump connected to the dehydration tower (28), and a seventh heater (30) connected to the seventh conveying pump.
2. The system for producing electronic isopropanol by the propylene hydration method according to claim 1, wherein: the crude isopropanol gas-liquid separator (12) and the crude isopropanol mixer (16) are connected with each other.
3. The system for producing electronic isopropanol by the propylene hydration method according to claim 1, wherein: the compressor (15) is connected with the raw material mixer (6).
4. The system for producing electronic isopropanol by the propylene hydration method according to claim 1, wherein: the second propylene hydration reactor (10) and the heat exchanger (7) are connected with each other.
5. The system for producing electronic isopropanol by the propylene hydration method according to claim 1, wherein: one side of the seventh heater (30) is connected with a seventh delivery pump, and the other side of the seventh heater is connected with the ethylene glycol feeding mixer (23).
6. The production method of the system for producing the electronic isopropanol by the propylene hydration method is characterized by comprising the following steps;
s1: pressurizing liquid propylene in a propylene feeding buffer tank (1) and water in a water feeding buffer tank (3) to 2.5MPa, then conveying the liquid propylene into a raw material mixer (6) by using a first conveying pump (2), conveying water into the raw material mixer (6) by using a second conveying pump (4) and a water feeding coarse mixer (5), mixing the water and the liquid propylene, then exchanging heat of the mixture by using a heat exchanger (7), heating the mixture of the water and the liquid propylene to 171 ℃ by using a first heater (8), and then enabling the mixture to sequentially enter a first propylene hydration reactor (9) and a second propylene hydration reactor (10) for reaction;
s2, after the liquid propylene reacts with water, a heat flow strand consisting of isopropanol and other side reactants is generated, the temperature of the heat flow strand flowing out of a second propylene hydration reactor (10) is reduced to 70 degrees after the heat flow strand passes through a heat exchanger (7) and a second heater (11), then the heat flow strand enters a gas-liquid separator to be subjected to gas-liquid separation operation, a gas flow and a liquid flow are formed after separation, the formed gas flow enters a crude isopropanol rectifying tower (13), the incompletely reacted flow exists at the top of the crude isopropanol rectifying tower (13) after rectification, the incompletely reacted flow enters the crude isopropanol knockout to be subjected to waste gas discharge, the incompletely reacted flow is pressurized by a compressor (15) and then flows back to a raw material mixer (6) to be mixed and reacted again, liquid can be distilled at the bottom of the crude isopropanol rectifying tower (13) after rectification, and the liquid flow generated in the gas-liquid separator flow into a crude isopropanol mixer (16) to be mixed;
s3: the mixed stream is heated by a third heater (17), then enters an isopropanol crude separation tower (18), waste gas is discharged from the top of the isopropanol crude separation tower (18), liquid at the bottom of the tower is heated to 105 ℃ by a fourth heater (19) and enters an isopropanol rectifying tower (20), waste liquid flows out from the bottom of the isopropanol rectifying tower (20), an isopropanol stream flows out from the top of the tower, then the isopropanol stream is conveyed into a fifth heater (22) by a third conveying pump (21) to be heated, and is conveyed into an extracting tower (24) to be extracted after being heated, meanwhile, ethylene glycol is conveyed into the extracting tower (24) by an ethylene glycol feeding mixer (23), residual azeotropic water in the isopropanol stream is extracted by the ethylene glycol, and the isopropanol is separated and purified;
s4: after extraction is finished, an isopropanol product flowing out of the top of the extraction tower (24) is pressurized to 0.7MPa through a fourth delivery pump (25), then is delivered to a sixth heater (27) to be condensed and cooled to 30 ℃, and then enters a storage tank for storage;
s5: after extraction is finished, the ethylene glycol extraction mixed solution flows out of the bottom of the extraction tower (24), the solution is pressurized to 0.7MPa through a fifth conveying pump (26) and then conveyed to a dehydration tower (28), waste water flows out of the top of the dehydration tower (28), ethylene glycol at the bottom of the tower is pressurized to 0.7MPa through a seventh conveying pump and then condensed and cooled to 40 ℃ through a seventh heater (30), and then the ethylene glycol enters an ethylene glycol feeding mixer (23), so that cyclic utilization of the ethylene glycol can be realized.
7. The method for producing the system for producing the electronic isopropanol by the propylene hydration method according to claim 6, wherein the method comprises the following steps: the operation pressure of the crude isopropanol rectifying tower (13) is 2.2MPa, the tower top temperature is 42 ℃, and the tower kettle temperature is 145 ℃.
8. The method for producing the system for producing the electronic isopropanol by the propylene hydration method according to claim 6, wherein the method comprises the following steps: the first propylene hydration reactor (9) has an operating pressure of 2.3MPa and an operating temperature of 170 ℃.
9. The method for producing the system for producing the electronic isopropanol by the propylene hydration method according to claim 6, wherein the method comprises the following steps: the operating temperature of the second propylene hydration reactor (10) is 210 ℃, and the operating pressure is 2.3MPa.
10. The system for producing electronic isopropanol by the propylene hydration method according to claim 6, wherein: the operating pressure of the extraction tower (24) is 0.18MPa, the tower top temperature is 88 ℃, and the tower kettle temperature is 174 ℃.
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