CN207451978U - A kind of device using carbon dioxide production n-propyl acetate - Google Patents
A kind of device using carbon dioxide production n-propyl acetate Download PDFInfo
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- CN207451978U CN207451978U CN201720571931.6U CN201720571931U CN207451978U CN 207451978 U CN207451978 U CN 207451978U CN 201720571931 U CN201720571931 U CN 201720571931U CN 207451978 U CN207451978 U CN 207451978U
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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
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model discloses a kind of devices using carbon dioxide production n-propyl acetate, using carbon dioxide as raw material, including raw material mixed cell, buffer cell, reaction member, waste heat recovery unit, quenching unit, compression unit, separative element, PSA unit, positive propionic aldehyde production unit, normal propyl alcohol production unit and n-propyl acetate production unit, carbon dioxide preparation ethylene, carbon monoxide, hydrogen and the raw material supply for producing its product as the positive propionic aldehyde in downstream, normal propyl alcohol, n-propyl acetate are utilized；Make fuel additional issue steam using technology waste gas, both the energy consumption of the present apparatus had been met, steam resource is saved again, has accomplished recycling for energy maximization, reduces pollutant emission, environmental protection and energy saving, subsequent technique provides raw material hydrogen for preceding technique, improves the conversion ratio of material, solves downstream unit and carrys out source problem to ethylene, hydrogen and carbon monoxide raw material, the perfect product diversification of enterprise, improves enterprise core competence.
Description
Technical field
The utility model is related to a kind of carbon dioxide discharge-reduction field more particularly to a kind of utilization carbon dioxide production acetic acid just
The device of propyl ester.
Background technology
With the development of modern industry, global Energy Consumption constantly increases severely, carbon dioxide (hereinafter referred to as CO2) discharge capacity
(in terms of carbon) is by 0.4 hundred million tons of develop to 1996 60.4 hundred million tons before the industrial revolution 1860.By 2100, global CO2Always
Discharge capacity is estimated to will be added to 36,000,000,000 tons.Countries in the world oneself notice that non-standing production of energy and development model make global ring
Border institute coming crisis in Western sociology.What in December, 1997 formulated《The Kyoto Protocol》, it is desirable that some industrialized countries in 2008-2012,
The discharge capacity of greenhouse gases is averagely reduced 5.2% on nineteen ninety horizontal base.These show：Most important greenhouse gases
CO2It is increasing with industrial expansion, exacerbate the deterioration of environment for human survival；Progressively the discharge of greenhouse gases is cut down
Through the common recognition for becoming most scientists and government organs.Thus, from the energy, carbon resource and mitigate CO2Environmental pollution etc.
Aspects considers, controls CO2Discharge and strengthen CO2Utilization be all one have great strategic significance problem.
CO2It is both most important greenhouse gases, while is also that one resource of carbon most wide, reserves are most abundant is distributed on the earth.
According to statistics with CO2With carbonate form existing for about 1016 tons of organic C storage, be explored coal and oil phosphorus content
1000 times.Also containing big in the manufacture gas of casing-head gas, synthesis ammonia, ironmaking, cement, fermentation, heat power station and device for producing hydrogen
The CO of amount2。CO2As a kind of widely used chemical products, beverage additive, supercritical extract agent, fruits and vegetables are may be directly applied to
Antistaling agent, low-temperature refrigerant, oil field adjuvant, welding protection gas, datonation-inhibition fill add agent, plant gas fertilizer, tobacco expanding agent, resin hair
The purposes such as infusion.In addition, CO2It, can be by CO by chemical process as important industrial chemicals2It is converted into higher economic valency
The product of value：Such as fine silica gel (white carbon), Boratex (borax), light magnesium oxide, propene carbonate, septichen
(salicylic acid), dicyandiamide (cyano flesh).
With CO2It is comprehensively utilized for raw material, on the one hand important raw material of industry ethylene can be provided, while can eliminated again
Cause the CO of greenhouse effects2, it is a catalytic reaction for having prospects for commercial application.Calculate analytical proof CO2Ethyl oxide dehydrogenation system
Ethylene reaction is thermodynamically highly advantageous.This is just research CO2Preparing ethene by oxidative dehydrogenation of ethane with provides theoretical foundation.
1987, Gnziev proposed CO2Presence can promote making ethylene from ethane oxidative dehydrogenation react after, both at home and abroad to CO2Aoxidize second
The ethylene reaction produced basic research work of alkane dehydrogenation has developed.
With CO2The new process comprehensively utilized for raw material has that reaction temperature is relatively low, low energy consumption, ethylene selectivity height etc.
Advantage.And the non-oil resources such as natural gas, casing-head gas can be fully applied, at home and abroad academia, industrial quarters cause extensively
Concern.CO2Application way is a green processes with environment and resource double benefit, and research is carried out to it with important
Scientific meaning and industrial application value.CO at present2It is industrialized mainly to include for the synthesis of chemicals：1st, urea 2, water
Poplar acid 3, cyclic carbonate 4, makrolon 5, methanol.The CO of industrial consumption2In, 90% contributes to the production of urea, product
Structure is more single, so the utilization and chemical conversion of carbon dioxide also need to further develop.It is domestic not yet to find to utilize CO2
The apparatus and method that large-scale production is carried out with ethane.
Positive propionic aldehyde and normal propyl alcohol are excellent organic solvent and important industrial chemicals, and wherein oxo synthesis is current
The main method of positive propionic aldehyde production, oxo synthesis also known as ethene hydroformylation method are using ethylene, carbon monoxide, hydrogen as original
Material, the method for generating propionic aldehyde under the effect of the catalyst, this method are mainly characterized by product purity height, and isomer-free generates,
Separation is easy, is the main method and developing direction for producing propionic aldehyde, and the production of normal propyl alcohol mainly includes two parts：Positive propionic aldehyde with
The subtractive process of thick propyl alcohol and thick propyl alcohol is made in hydrogen reaction, and raw material is positive propionic aldehyde and hydrogen.
And the product of above-mentioned preparing ethene by oxidative dehydrogenation of ethane with carbon dioxide reaction contains all positive propionic aldehyde and just
The raw material of propyl alcohol production, if can reasonably recycle it will bring very big economic benefit and environmental benefit, example
It such as preparing positive propionic aldehyde, is further continued for recycling the production for carrying out normal propyl alcohol, then further original low with some conventional valencys
Material as acetic acid react jointly carry out n-propyl acetate industrialized production, it will be an environmental protection and energy saving and reduction enterprise's raw material into
This major action.
Utility model content
Purpose of utility model：In order to solve the problems of in the prior art, the utility model proposes a kind of environment
Friendly, various materials resource and energy recycling, reduce the discharge of pollutant, and environment-friendly high-efficiency enriches enterprise product structure
Utilize the device of carbon dioxide production n-propyl acetate.
Technical solution：To achieve these objectives, the utility model takes following technical scheme：It is a kind of to utilize carbon dioxide production
The device of n-propyl acetate includes raw material mixed cell, buffer cell, reaction member, waste heat recovery list successively by reaction step
Member, quenching unit, compression unit, separative element, PSA unit, positive propionic aldehyde production unit, normal propyl alcohol production unit and acetic acid are just
Propyl ester production unit；
Wherein described reaction member is the reacting furnace with feed preheater；There is reaction boiler tube in the reacting furnace；
The waste heat recovery unit includes level-one waste heat boiler and two level waste heat boiler；
The quenching unit is the chilling tower for including tower top liquid separation tank, bottom of towe chilling water pump and bottom of towe filter；
The compression unit include one stage of compression system, absorption tower decarbonization system, regeneration Tower System, de- benzene drying system with
And two-stage compression system；
The separative element includes ice chest, domethanizing column system, ethylene Tower System and dethanizer system；The piptonychia
Alkane Tower System bottom of towe is connected with reboiler；The ethylene Tower System is Shang Ta and the cold separated structure of lower tower heat, wherein upper tower passes through
Ethylene pump is connected with ethylene tank；
The positive propionic aldehyde production unit includes ethylene synthase gas cleaning system, primary heater, hydrogen successively by reaction process
Formylation reaction kettle, the first cooler, liquid liquid stratification tank, first rectifying column, the first grease phase-splitter and the first recycling
Tower；First cooler is also associated with knockout drum；
The normal propyl alcohol production unit includes secondary heater, hydrogenation reactor, knockout drum, second successively by reaction process
Rectifying column, second recovery column；The first condenser and Xun Huan oxygen compressor, the cycling oxygen is also respectively connected in the knockout drum
The compressor other end is connected to hydrogenation reactor；
The n-propyl acetate production unit is included feed preheater, reaction kettle of the esterification, second cold by reaction process successively
But device, phase-splitter, water scrubber, dehydrogenation tower, third distillation column and the 3rd recovery tower；The water scrubber is also associated with the second condensation
Device；Described third distillation column one end is also connected with the second grease phase-splitter, and the second grease phase-splitter is connected with water mutually at recycling
Device is managed, the water is mutually recycled device and is equipped with the organic phase recovery channel for leading to reaction kettle of the esterification；
Wherein, three feeding streams ethane and cycle ethane, carbon dioxide and Xun Huan carbon dioxide, water steam in raw material mixed cell
Gas enters buffer cell after being mixed, and subsequently enters in reaction member and is reacted；Generate major product ethylene and an oxidation
Carbon, hydrogen, methane, C3+The byproducts such as hydro carbons, water；Reacting furnace exit gas is pyroprocess gas, subsequently enters waste heat recovery list
Member carries out hair vapour, and byproduct is recycled as the fuel of the present apparatus；Cycle ethane comes from later separation unit deethanization
Tower System Reaction Separation carries out cycling and reutilization；It is sharp again to cycle cycling of the carbon dioxide from compression unit regeneration Tower System outlet
With；Vapor takes off benzene drying system from compression unit and carries out cycling and reutilization；
Pyroprocess gas from reaction member, after sending out vapour conduct after level-one waste heat boiler into waste heat recovery unit
Continuous compression unit compressibility heat source uses；Vapour is sent out after two level waste heat boiler as subsequent compression regeneration unit Tower System heat source
It uses；
Pyroprocess gas after waste heat recovery unit enters next stage compression unit after entering quenching unit；Chilling bottom of towe
It is used after the chilling water section processing of end as later separation unit heat source；
Then Process Gas after cooling continues pressurization through one stage of compression system, decarburization, de- benzene, drying, two-stage compression system
Into next stage separative element；
The Process Gas come from compression unit exchanges heat first with domethanizing column system materials at bottom of tower, Process Gas after liquid separation into
Enter ice chest heat exchange progressively to cool down, ice chest bottom liquid is directly as the charging of domethanizing column system, and ice chest top gas phase is as thick
Synthesis gas enters follow-up PSA unit；
Domethanizing column system bottom of towe is using chilled water (chw) as reboiler heat source, bottom of towe C2+After material exchanges heat with fill process gas
Ethylene Tower System, ice chest top gas phase and domethanizing column system top are entered back into after C2 hydrogenation system processing removal acetylene impurities
Gas merges, and PSA unit is entered after heating；
C after hydrogenated2+Material is directly entered tower under ethylene column, and fixed gas enters after pressure controls in ethylene Tower System
Compression unit Xun Huan is compressed utmostly to recycle ethylene；Pumped ethylene is sent out with ethylene, send to ethylene tank and stores；Recycle second
C after alkene2+Material enters dethanizer system at ethylene column bottom after pressure controls；Reflux of the condensed liquid as tower,
Fixed gas, that is, cycle ethane initially enters ice chest recycling cold after pressure controls, is used after heating as reaction raw materials；Bottom of towe
Material is C3+, be divided into two-way after water cooling, all the way it is pressurized continue cooling after used as the cleaning solution for taking off benzene drying system, in addition
It is used all the way directly as device or residual neat recovering system fuel；
Crude synthesis gas enters PSA unit, after gas-liquid separator by pressure swing adsorption system PSA obtain hydrogen purity >=
99.99% product hydrogen, product hydrogen export out-of-bounds；PSA resolution gas is sent out out-of-bounds；The resolution gas is after processing as synthesis
Gas raw material is used for downstream, with other products of device collectively as the reaction raw materials of positive propionic aldehyde production unit；
After the compressed boosting of synthesis gas and ethylene, heating from leading portion reaction carbonyl is carried out into hydroformylation reaction kettle
Base synthetic reaction, the reaction heat of generation are taken away through the cooling of outer circulation cooler；After the completion of reaction, reaction product is first through the first cooling
Into liquid liquid stratification tank and knockout drum after device cooling, the former separates water outlet phase and returns system circulation utilization, organic phase warp
Rectifying column obtains qualified positive propionic aldehyde, raw materials for production of the part as subsequent downstream product, and a part carries out outer sell as product；
The separated gas phase of knockout drum is utilized as device fuel recycle simultaneously, and liquid phase after cooling returns to liquid liquid stratification tank；
Waste liquid of the bottom of towe containing a large amount of water mutually directly returns hydroformylation reaction kettle into separation water outlet through the first grease phase-splitter and recycles, oil
First recovery column is mutually gone to recycle；
The positive propionic aldehyde that positive propionic aldehyde production unit rectifying obtains, after being mixed with one of PSA unit product hydrogen, through the second heating
Gas-liquid is carried out in knockout drum after heat exchange cools down into hydrogenation reactor, the thick normal propyl alcohol of reaction product after device heat exchange evaporation
It separates, hydrogen enters circulating hydrogen compressor in gas phase, and the use of hydrogenation reactor system circulation, foreign gas warp are entered back into after supercharging
After ethylene glycol freezing liquid deep cooling ground flare is finally gone to burn in first condenser, condensate liquid returns knockout drum, and liquid phase then sends to the
Two rectifying columns, tower top obtain qualified normal propyl alcohol product, and fixed gas is used as device fuel；A normal propyl alcohol part is produced as downstream
The raw materials for production of product, a part are used as commodity normal propyl alcohol export trade；Bottom of towe rectifying liquid is sent to second recovery column and is recycled；
The normal propyl alcohol and acetic acid that normal propyl alcohol production unit rectifying obtains enter after feed preheater heats equipped with organic acid
Reaction in the reaction kettle of the esterification of catalyst, after extra water is separated through phase-splitter after the cooling of reaction product liquid phase into water scrubber into
Row washing, obtains thick ester, fixed gas is used as device fuel；Thick ester continues rectifying into lightness-removing column, light group come out from tower top
Return reaction kettle of the esterification is divided to continue with, torch burning is finally removed after fixed gas deep cooling；The component that bottom of towe comes out is smart into the 3rd
It evaporates tower and carries out secondary rectifying, the product that tower top comes out is final n-propyl acetate product, and fixed gas is used as device fuel；
Tower reactor restructuring dispensing to the 3rd recovery tower rectifying is recycled, and the water phase centralized collection that the second grease phase-splitter and water scrubber separate is laggard
Entering water and be mutually recycled device to carry out concentration batch distillation, the organic phase overwhelming majority, which is distilled to recover to reaction kettle of the esterification, to be recycled,
Last water phase sewage treatment.
It is more highly preferred to, the reacting furnace is vertical batch-type furnace.
Advantageous effect：A kind of device using carbon dioxide production n-propyl acetate provided by the utility model, have with
Lower advantage：
(a) technology comprehensively utilized using carbon dioxide as raw material, be ethane conversion and carbon dioxide utilize it is effective
Approach, not only for alleviating energy crisis, the production process and raw material route for changing some chemical products have great reality
Meaning, and the discharge to reducing greenhouse gases have far-reaching history caused by mitigating " greenhouse effects " to global ecological environment
Meaning.
(b) comprehensively utilized by raw material of carbon dioxide, it is former to ethylene, hydrogen and carbon monoxide to solve downstream unit
Material carrys out source problem, and the perfect product diversification of enterprise not only has ethylene principal product, moreover it is possible to make full use of former among various
Material, carries out a series of preparation of downstream product for example positive propionic aldehyde, normal propyl alcohol, n-propyl acetate, improves enterprise core competence.
(c) comprehensively utilized by raw material of carbon dioxide, employ environmentally friendly technology, taken effective environmental protection and arrange
It applies, particularly fixed carbon dioxide is substituted coal chemical industry, met using carbon dioxide preparation ethylene, carbon monoxide and hydrogen
The production of industry.
(d) make fuel additional issue steam using exhaust gas caused by technique, not only met the energy requirements of the present apparatus, but also saved
Steam resource, has accomplished energy recycling as far as possible, reduces pollutant discharge amount and concentration of emission, and meeting environmental protection will
It asks.
(e) various materials are taken in this technology, and either scrap loop is used or utilized, and avoids the waste of the energy：
Including A) by the use of waste heat as the heat source of subsequent technique；Fully recycling preheating reduces wastage in bulk or weight, cost-effective；B waste material) is utilized
C3+As detergent and fuel；C) carbon dioxide and ethane recovery recycle, and avoid pollution air and energy waste；D it is) follow-up
Technique provides raw material hydrogen for previous process, improves the conversion ratio of material, avoids pollution air and energy waste；E) reaction production
Raw water recycles after subsequent technique extracts back to raw material, avoids generation and the water resource waste of waste water；F it is) anti-
Raw materials for production of the synthesis gas of one of product as the positive propionic aldehyde device in downstream are answered, and make full use of the positive propionic aldehyde of intermediate product and hydrogen
Gas carries out the preparation of downstream product normal propyl alcohol, and further raw material such as acetic acid low with some routine valencys is reacting jointly is carrying out acetic acid just
The industrialized production of propyl ester, environmental protection and energy saving reduce entreprise cost, and high conversion rate, high selectivity, remarkable in economical benefits.
Description of the drawings
Fig. 1 is that a kind of device flow using carbon dioxide production n-propyl acetate of the utility model specific embodiment is illustrated
Figure；
Fig. 2 is a kind of the first eight unit of device using carbon dioxide production n-propyl acetate of the utility model specific embodiment
Decomposition process schematic diagram；
Fig. 3 is the positive propionic aldehyde of the utility model specific embodiment, normal propyl alcohol and n-propyl acetate production unit device and life
Produce flow diagram.
Specific embodiment
Embodiment 1：
Fig. 1 is refer to, the utility model discloses a kind of device using carbon dioxide production n-propyl acetate, by reaction
Step includes raw material mixed cell 1, buffer cell 2, reaction member 3, waste heat recovery unit 4, quenching unit 5, compression list successively
Member 6, separative element 7, PSA unit 8, positive propionic aldehyde production unit 9, normal propyl alcohol production unit 10 and n-propyl acetate production unit
11；
It refers to shown in Fig. 2, wherein the reaction member 3 is the reacting furnace 31 with feed preheater；The reacting furnace
There is reaction boiler tube 32 in 31；The reacting furnace 31 is vertical batch-type furnace；
The waste heat recovery unit 4 includes level-one waste heat boiler 41 and two level waste heat boiler 42；
The quenching unit 5 is to include tower top liquid separation tank 51, bottom of towe chilling water pump 52 and bottom of towe filter (not shown)
Chilling tower；
The compression unit 6, which includes one stage of compression system 61, absorption tower decarbonization system 62, regeneration Tower System 63, de- benzene, to be done
Drying system 64 and two-stage compression system 65；
The separative element 7 includes ice chest 71, domethanizing column system 72, ethylene Tower System 73 and dethanizer system
74；72 bottom of towe of domethanizing column system is connected with reboiler 721；The ethylene Tower System 73 is 732 heat of upper tower 731 and lower tower
Cold separated structure, wherein upper tower 731 is connected with ethylene tank 734 by ethylene pump 733；
The positive propionic aldehyde production unit includes ethylene synthase gas cleaning system 91, primary heater successively by reaction process
92nd, hydroformylation reaction kettle 93, the first cooler 94, liquid liquid stratification tank 95, first rectifying column 97, the first grease phase-splitter
98 and first recovery column 99；First cooler 94 is also associated with knockout drum 96；
The normal propyl alcohol production unit 10 is included secondary heater 101, hydrogenation reactor 102 by reaction process, divided successively
From tank 103, Second distillation column 105, second recovery column 106；The knockout drum 103 be also respectively connected the first condenser 107 with
And Xun Huan oxygen compressor 104, Xun Huan 104 other end of oxygen compressor are connected to hydrogenation reactor 102；
The n-propyl acetate production unit 11 includes feed preheater 111, reaction kettle of the esterification successively by reaction process
112nd, the second cooler 113, phase-splitter 114, water scrubber 115, dehydrogenation tower 117,118 and the 3rd recovery tower of third distillation column
119；The water scrubber 115 is also associated with the second condenser 116；Described 118 one end of third distillation column is also connected with the second grease point
Phase device 120, the second grease phase-splitter 120 are connected with water and are mutually recycled device 121, and the water is mutually recycled device 121 and sets
There is the organic phase recovery channel for leading to reaction kettle of the esterification 112.
Based on above-mentioned device, a kind of method using carbon dioxide production n-propyl acetate, including following reaction process：
(1) raw material mixed cell 1, buffer cell 2 and reaction member 3：Three feeding streams are mixed in raw material mixed cell 1
It closes, first burst of charging is ethane and cycle ethane, and second burst of charging is carbon dioxide and Xun Huan carbon dioxide, and three feeding streams are
Vapor；Three feeding streams into buffer cell 2, subsequently enter the feed preheater in reaction member 3, are preheated to upon mixing
After 50-500 DEG C temperature reaction is carried out into reacting furnace 31；Equipped with ethane dehydrogenation catalyst in reaction boiler tube 32,500- is warming up to
1500 DEG C, ethane, carbon dioxide, vapor react under the effect of the catalyst, generate major product ethylene；And carbon monoxide,
Hydrogen, methane, C3+The byproducts such as hydro carbons, water；Reacting furnace 31 keeps reaction temperature, and reaction is enable to be carried out towards beneficial direction；Instead
31 exit gas of stove is answered to subsequently enter next unit waste heat recovery unit 4 for pyroprocess gas and carry out hair vapour, byproduct is a small amount of
Methane and C3+Hydro carbons is recycled as the fuel of the present apparatus；
Cycle ethane wherein in three feeding streams is followed from 7 dethanizer system of later separation unit, 74 Reaction Separation
Ring recycles；Cycle the cycling and reutilization that carbon dioxide regenerates 63 outlet of Tower System from compression unit 6；Vapor is from compression
Unit 6 takes off benzene drying system 64 and carries out cycling and reutilization；
(2) waste heat recovery unit 4 and quenching unit 5：Pyroprocess gas from reaction member 3, temperature 550-1200
DEG C, into the level-one waste heat boiler 41 of waste heat recovery unit 4 after send out 1-10MPa grades saturated vapor, into reacting furnace flue
Overheat, uses as 6 compressibility heat source of subsequent compression unit；Pass through the pyroprocess gas after level-one waste heat boiler 41, temperature
For 200-800 DEG C, into two level waste heat boiler 42 after send out 0.1-1.0MPa grades saturated vapor, as subsequent compression unit 6
63 heat source of Tower System is regenerated to use；
Pyroprocess gas after two-stage waste heat boiler is cooled to 50-400 DEG C and enters quenching unit 5, in chilling tower,
Pyroprocess gas and chilled water (chw) counter current contacting are cooled to 10-100 DEG C of Process Gas and enter tower top liquid separation tank 51, subsequently enter down
One stage of compression unit 6；Chilling bottom of towe end chilled water (chw) partly filters removal reaction life after the supercharging of chilling water pump 52 by filter
Into coke impurity, consequently as 7 heat source of later separation unit use；
(3) compression unit 6：In one stage of compression system 61, the Process Gas after cooling is pressurized to by 0.01Mpa-1.0Mpa
1Mpa-10MPa；Decarburization is carried out into absorption tower decarbonization system 62；MDEA solution is wherein used as absorbent, absorption process gas
In carbon dioxide, the MDEA rich solvents after absorbing carbon dioxide enter regeneration Tower System 63 and regenerate, and regeneration Tower System 63 uses
Conventional stripping process；Rich solvent regenerates after rich or poor solvent heat exchanger exchanges heat to 20-200 DEG C or so into regenerator system 63,
It works off one's feeling vent one's spleen and is used as pressurized send to reacting furnace 31 of Xun Huan carbon dioxide as raw material；De- benzene drying system 64 uses washers
Skill, using the C that later separation unit 7 is self-produced3+It is washed, C in the Process Gas after washing6H6Content≤100ppm；Through decarburization,
De- benzene, dried Process Gas enter two-stage compression system 65, continue to be forced into after 1Mpa-10MPa separating list into next stage
Member 7；
(4) separative element 7：It exchanges heat first with 72 materials at bottom of tower of domethanizing column system from the Process Gas of compression unit 6, warp
Process Gas after liquid separation enters ice chest 71, and in ice chest 71, Process Gas is progressively cooled to -50--5 with cryogen and synthesis gas heat exchange
DEG C, 71 bottom liquid of ice chest is directly as the charging of domethanizing column system 72, and 71 top gas phase of ice chest is as crude synthesis gas entrance
Follow-up PSA unit 8；
72 bottom of towe of domethanizing column system is using chilled water (chw) as 721 heat source of reboiler, bottom of towe C2+Material and fill process gas
After heat exchange ethylene Tower System 73,71 top gas phase of ice chest and piptonychia are entered back into after C2 hydrogenation system processing removal acetylene impurities
72 top gas of alkane Tower System merges, and PSA unit 8 is entered after being warming up to 1 DEG C -80 DEG C；
C after hydrogenated2+Material is directly entered 73 times towers of ethylene Tower System 732, and 73 times towers of ethylene Tower System, 732 bottom of towe is adopted
By the use of chilled water (chw) as heat source, upper 731 tower top of tower is using refrigerant as low-temperature receiver；With -50 DEG C -- 5 DEG C of refrigerant condensation coolings, it is cold
Reflux of the liquid as tower after solidifying, fixed gas compress utmostly to recycle after pressure controls into the Xun Huan of compression unit 6
Ethylene；733 extraction ethylene of pump is sent out with ethylene, send to ethylene tank 734 and stores；Recycle the C after ethylene2+Material at ethylene column bottom,
Enter dethanizer system 74 after exchanging heat after pressure controls with 74 materials at bottom of tower of dethanizer system；74 tower of dethanizer system
Using chilled water (chw) as heat source, tower top has low-temperature receiver at bottom；Reflux of the condensed liquid as tower, fixed gas, that is, cycle ethane, warp
Ice chest 71 is initially entered after pressure control and recycles cold, is used after being warming up to 10-70 DEG C as reaction raw materials；Materials at bottom of tower is C3 +, water cooling is pressurized all the way to continue to be cooled to washing as de- benzene drying system 64 after 5-50 DEG C to two-way is divided into after 15-65 DEG C
Liquid use is washed, is in addition used all the way directly as device or 4 fuel of waste heat recovery unit；
(5) PSA unit 8：Crude synthesis gas enters PSA unit 8 at 1Mpa-10Mpa, 1 DEG C -80 DEG C, by gas-liquid separation
The product hydrogen of hydrogen purity >=99.00% is obtained by pressure swing adsorption system PSA after device, product hydrogen exports out-of-bounds；PSA is parsed
Gas is sent out out-of-bounds under 0.01MP-0.1MPa；The resolution gas uses after processing as raw material of synthetic gas for downstream, with device
Other products are collectively as the reaction raw materials of positive propionic aldehyde production unit；
(6) positive propionic aldehyde synthesis unit 9：Fig. 3 is refer to, synthesis gas and ethylene from leading portion reaction are through ethylene synthase gas
50-80 DEG C is heated to through primary heater 92 after the processing boosting of cleaning system 91, is carried out into hydroformylation reaction kettle 93
Carbongl group synthesis reaction, the reaction heat of generation are taken away through the cooling of outer circulation cooler, with continuously entering for material, reaction continuously into
Row, controlled at 80-150 DEG C, pressure 0.5-5Mpa；After the completion of reaction, reaction product first cools down through the first cooler 94
Afterwards into liquid liquid stratification tank 95 and knockout drum 96, water mutually returns after stratification wherein in liquid liquid stratification tank 95
System circulation utilizes, and organic phase goes first rectifying column 97, and tower top obtains qualified positive propionic aldehyde, and a part is as subsequent downstream product
Raw materials for production, a part carry out outer sell as product；96 separated gas phase of knockout drum is as device fuel recycle profit simultaneously
With liquid phase after cooling returns to liquid liquid stratification tank 95；Waste liquid of the bottom of towe containing a large amount of water first through the first grease phase-splitter 98 into
Row split-phase, wherein water are mutually directly returned hydroformylation reaction kettle 93 and are recycled, and oil phase goes first recovery column 99 to recycle, this conjunction
It is more than 99% into positive propionic aldehyde reaction conversion ratio TRC is reacted；
(7) normal propyl alcohol production unit 10：The positive propionic aldehyde that positive 10 rectifying of propionic aldehyde production unit obtains, one with PSA unit 8
After hydrogen product mixing, enter hydrogenation reactor 102, hot spot reaction temperature and pressure after the heat exchange evaporation of secondary heater 101
It is controlled respectively at 100-300 DEG C and 0.1-1Mpa；The thick normal propyl alcohol of reaction product is by heat exchange and is cooled to 5-50 DEG C, is separating
Gas-liquid separation is carried out in tank 103, is largely hydrogen in gas phase, into circulating hydrogen compressor 104, it is anti-that hydrogenation is entered back into after supercharging
Device system 102 is answered to recycle, a small amount of foreign gas finally goes to ground after the first condenser 107 carries out ethylene glycol freezing liquid deep cooling
Face torch burning, condensate liquid return knockout drum 103, and liquid phase then sends to Second distillation column 105, and tower top obtains qualified normal propyl alcohol product,
Fixed gas is used as device fuel；Raw materials for production of the which part normal propyl alcohol as downstream product, remaining is as commodity positive third
Alcohol export trade；Bottom of towe rectifying liquid is sent to second recovery column 106 and is recycled；
(8) n-propyl acetate production unit：The normal propyl alcohol raw material and acetic acid that 10 rectifying of normal propyl alcohol production unit is obtained lead to
It crosses conveying to be pumped into feed preheater 111 and heated, preheating temperature is controlled between 50~150 DEG C, by the mixing of preheating
Liquid is entered in the reaction kettle of the esterification 112 equipped with organic acid catalyst, is reacted under 100~200 DEG C of temperature, normal pressure, instead
After product liquid phase is answered to separate extra water through phase-splitter 114 after the cooling of the second cooler 113 water is carried out into water scrubber 115
It washes, removes most of propyl alcohol and obtain thick ester, wherein fixed gas is used as device fuel；Thick ester after washing separates enters
Lightness-removing column 117 continues rectifying, the light component come out from tower top, and it is anti-to return to esterification containing normal propyl alcohol, water and a small amount of n-propyl acetate
Kettle is answered to continue with, fixed gas finally removes torch burning after 116 ethylene glycol freezing liquid deep cooling of the second condenser；What bottom of towe came out
Component contains substantial amounts of n-propyl acetate and a small amount of acetic acid and other heavy constituents, and secondary fine is carried out into third distillation column 118
It evaporates, the product that tower top comes out is final n-propyl acetate product, is delivered to finished product storage tank, fixed gas makes as device fuel
With；Tower reactor heavy constituent is delivered to 119 rectifying of the 3rd recovery tower recycling by column bottoms pump, is separated via the second grease phase-splitter 120
The water phase that water phase and water scrubber 115 wash out mutually is recycled device 121 into water after centralized collection and carries out concentration batch distillation, steaming
The top temperature control system of tower is evaporated at 100 DEG C -200 DEG C and maintains 1-5h, and the organic phase overwhelming majority is distilled to recover to reaction kettle of the esterification 112
It recycles, last water is mutually discharged into sewage-treatment plant.
The present apparatus takes various materials, and either scrap loop is used or utilized, and avoids the waste of the energy：Including
A) by the use of waste heat as the heat source of subsequent technique；Fully recycling preheating reduces wastage in bulk or weight, cost-effective；B waste material C) is utilized3+Make
For detergent and fuel；C) carbon dioxide and ethane recovery recycle, and avoid pollution air and energy waste；D) subsequent technique
Raw material hydrogen is provided for previous process, improves the conversion ratio of material, avoids pollution air and energy waste；E) reaction generates
Water recycles after subsequent technique extracts back to raw material, avoids generation and the water resource waste of waste water；F) reaction production
Raw materials for production of the synthesis gas of one of product as the positive propionic aldehyde device in downstream, and make full use of the positive propionic aldehyde of intermediate product and hydrogen into
The preparation of row downstream product normal propyl alcohol, further raw material such as acetic acid low with some conventional valencys react carry out n-propyl acetate jointly
Industrialized production, environmental protection and energy saving reduce entreprise cost, and high conversion rate, high selectivity, remarkable in economical benefits.
It should be pointed out that for those skilled in the art, before the utility model principle is not departed from
It puts, several improvement can also be made, these improvement also should be regarded as the scope of protection of the utility model.
Claims (2)
1. a kind of device using carbon dioxide production n-propyl acetate, it is characterised in that mixed successively including raw material by reaction step
Close unit (1), buffer cell (2), reaction member (3), waste heat recovery unit (4), quenching unit (5), compression unit (6), point
It is produced from unit (7), PSA unit (8), positive propionic aldehyde production unit (9), normal propyl alcohol production unit (10) and n-propyl acetate single
First (11)；
Wherein described reaction member (3) is the reacting furnace (31) with feed preheater；There is reacting furnace in the reacting furnace (31)
It manages (32)；
The waste heat recovery unit (4) includes level-one waste heat boiler (41) and two level waste heat boiler (42)；
The quenching unit (5) is the chilling tower of tower top liquid separation tank (51), bottom of towe chilling water pump (52) and bottom of towe filter；
The compression unit (6) includes one stage of compression system (61), absorption tower decarbonization system (62), regenerates Tower System (63), is de-
Benzene drying system (64) and two-stage compression system (65)；
The separative element (7) includes ice chest (71), domethanizing column system (72), ethylene Tower System (73) and dethanizer system
It unites (74)；Domethanizing column system (72) bottom of towe is connected with reboiler (721)；The ethylene Tower System (73) is upper tower
(731) the cold separated structure of He Xiata (732) heat, wherein upper tower (731) pumps (733) by ethylene and is connected with ethylene tank (734)；
The positive propionic aldehyde production unit (9) includes ethylene synthase gas cleaning system (91), primary heater successively by reaction process
(92), hydroformylation reaction kettle (93), the first cooler (94), liquid liquid stratification tank (95), first rectifying column (97), first
Grease phase-splitter (98) and first recovery column (99)；First cooler (94) is also associated with knockout drum (96)；
The normal propyl alcohol production unit (10) by reaction process successively include secondary heater (101), hydrogenation reactor (102),
Knockout drum (103), Second distillation column (105), second recovery column (106)；It is cold that the knockout drum (103) is also respectively connected first
Condenser (107) and Xun Huan oxygen compressor (104), described Xun Huan oxygen compressor (104) other end are connected to hydrogenation reactor
(102)；
The n-propyl acetate production unit (11) includes feed preheater (111), reaction kettle of the esterification successively by reaction process
(112), the second cooler (113), phase-splitter (114), water scrubber (115), dehydrogenation tower (117), third distillation column (118) and
3rd recovery tower (119)；The water scrubber (115) is also associated with the second condenser (116)；The third distillation column (118) one
End is also connected with the second grease phase-splitter (120), and the second grease phase-splitter (120) is connected with water and is mutually recycled device (121),
The water is mutually recycled device (121) and is equipped with the organic phase recovery channel for leading to reaction kettle of the esterification (112)；
Wherein, three feeding streams ethane and cycle ethane, carbon dioxide and cycle carbon dioxide in raw material mixed cell, vapor into
Into buffer cell after row mixing, subsequently enter in reaction member and reacted；Generate major product ethylene and carbon monoxide,
Hydrogen, methane, C3+The byproducts such as hydro carbons, water；Reacting furnace exit gas be pyroprocess gas, subsequently enter waste heat recovery unit into
Row hair vapour, byproduct are recycled as the fuel of the present apparatus；Cycle ethane comes from later separation unit dethanizer system
Reaction Separation of uniting carries out cycling and reutilization；Cycle cycling and reutilization of the carbon dioxide from compression unit regeneration Tower System outlet；
Vapor takes off benzene drying system from compression unit and carries out cycling and reutilization；
Pyroprocess gas from reaction member sends out vapour as follow-up pressure into waste heat recovery unit after level-one waste heat boiler
Contracting cell compression system heat sources use；Vapour is sent out after two level waste heat boiler to be made as subsequent compression regeneration unit Tower System heat source
With；
Pyroprocess gas after waste heat recovery unit enters next stage compression unit after entering quenching unit；Chilling bottom of towe end is anxious
It is used after the processing of cold water part as later separation unit heat source；
Process Gas after cooling through one stage of compression system, decarburization, de- benzene, drying, two-stage compression system, continue pressurization subsequently into
Next stage separative element；
The Process Gas come from compression unit exchanges heat first with domethanizing column system materials at bottom of tower, and the Process Gas after liquid separation enters cold
Case heat exchange progressively cools down, and ice chest bottom liquid is directly as the charging of domethanizing column system, and ice chest top gas phase is as thick synthesis
Gas enters follow-up PSA unit；
Domethanizing column system bottom of towe is using chilled water (chw) as reboiler heat source, bottom of towe C2+Through carbon after material and the heat exchange of fill process gas
Ethylene Tower System is entered back into after two hydrogenation systems processing removal acetylene impurities, ice chest top gas phase and domethanizing column system top gas are closed
And enter PSA unit after heating；
C after hydrogenated2+Material is directly entered tower under ethylene column, and fixed gas enters compression after pressure controls in ethylene Tower System
Unit Xun Huan is compressed utmostly to recycle ethylene；Pumped ethylene is sent out with ethylene, send to ethylene tank and stores；After recycling ethylene
C2+Material enters dethanizer system at ethylene column bottom after pressure controls；Reflux of the condensed liquid as tower, does not coagulate
Gas, that is, cycle ethane initially enters ice chest recycling cold after pressure controls, is used after heating as reaction raw materials；Materials at bottom of tower
For C3+, be divided into two-way after water cooling, all the way it is pressurized continue cooling after used as the cleaning solution for taking off benzene drying system, in addition all the way
It is used directly as device or residual neat recovering system fuel；
Crude synthesis gas enters PSA unit, after gas-liquid separator by pressure swing adsorption system PSA obtain hydrogen purity >=
99.99% product hydrogen, product hydrogen export out-of-bounds；PSA resolution gas is sent out out-of-bounds；The resolution gas is after processing as synthesis
Gas raw material is used for downstream, with other products of device collectively as the reaction raw materials of positive propionic aldehyde production unit；
After the compressed boosting of synthesis gas and ethylene, heating from leading portion reaction carbonyl conjunction is carried out into hydroformylation reaction kettle
Into reaction, the reaction heat of generation is taken away through the cooling of outer circulation cooler；After the completion of reaction, reaction product is first dropped through the first cooler
Into liquid liquid stratification tank and knockout drum after temperature, the former separates water outlet phase and returns system circulation utilization, and organic phase is through rectifying
Tower obtains qualified positive propionic aldehyde, raw materials for production of the part as subsequent downstream product, and a part carries out outer sell as product；Simultaneously
The separated gas phase of knockout drum is utilized as device fuel recycle, and liquid phase after cooling returns to liquid liquid stratification tank；Bottom of towe
Waste liquid containing a large amount of water mutually directly returns hydroformylation reaction kettle into separation water outlet through the first grease phase-splitter and recycles, and oil phase is gone
First recovery column recycles；
The positive propionic aldehyde that positive propionic aldehyde production unit rectifying obtains, after being mixed with one of PSA unit product hydrogen, is changed through secondary heater
Into hydrogenation reactor after thermal evaporation, the thick normal propyl alcohol of reaction product carries out gas-liquid point after heat exchange cools down in knockout drum
From hydrogen enters circulating hydrogen compressor in gas phase, the use of hydrogenation reactor system circulation is entered back into after supercharging, foreign gas is through the
After ethylene glycol freezing liquid deep cooling ground flare is finally gone to burn in one condenser, condensate liquid returns knockout drum, and liquid phase then sends to second
Rectifying column, tower top obtain qualified normal propyl alcohol product, and fixed gas is used as device fuel；A normal propyl alcohol part is used as downstream product
Raw materials for production, a part be used as commodity normal propyl alcohol export trade；Bottom of towe rectifying liquid is sent to second recovery column and is recycled；
The normal propyl alcohol and acetic acid that normal propyl alcohol production unit rectifying obtains enter after feed preheater heats equipped with organic acid catalysis
Reaction in the reaction kettle of the esterification of agent carries out water after extra water is separated through phase-splitter after the cooling of reaction product liquid phase into water scrubber
It washes, obtains thick ester, fixed gas is used as device fuel；Thick ester continues rectifying into lightness-removing column, and the light component come out from tower top is returned
It returns reaction kettle of the esterification to continue with, torch burning is finally removed after fixed gas deep cooling；The component that bottom of towe comes out enters third distillation column
Secondary rectifying is carried out, the product that tower top comes out is final n-propyl acetate product, and fixed gas is used as device fuel；Tower reactor
Restructuring dispensing to the 3rd recovery tower rectifying is recycled, and water is entered after the water phase centralized collection that the second grease phase-splitter and water scrubber separate
Mutually recovery processing device carries out concentration batch distillation, and the organic phase overwhelming majority, which is distilled to recover to reaction kettle of the esterification, to be recycled, finally
Water phase sewage treatment.
2. the device according to claim 1 using carbon dioxide production n-propyl acetate, it is characterised in that：The reaction
Stove (31) is vertical batch-type furnace.
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| CN201720571931.6U CN207451978U (en) | 2017-05-22 | 2017-05-22 | A kind of device using carbon dioxide production n-propyl acetate |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112441877A (en) * | 2020-11-13 | 2021-03-05 | 四川新火炬化工有限责任公司 | Method and system for preparing ethylene glycol (OD)2 |
| CN115138303A (en) * | 2022-07-07 | 2022-10-04 | 南京荣欣化工有限公司 | Device for preparing n-propyl acetate from carbon dioxide and preparation method thereof |
-
2017
- 2017-05-22 CN CN201720571931.6U patent/CN207451978U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112441877A (en) * | 2020-11-13 | 2021-03-05 | 四川新火炬化工有限责任公司 | Method and system for preparing ethylene glycol (OD)2 |
| CN112441877B (en) * | 2020-11-13 | 2023-06-02 | 四川新火炬化工有限责任公司 | Preparation method and preparation system of ethylene glycol (OD) 2 |
| CN115138303A (en) * | 2022-07-07 | 2022-10-04 | 南京荣欣化工有限公司 | Device for preparing n-propyl acetate from carbon dioxide and preparation method thereof |
| CN115138303B (en) * | 2022-07-07 | 2023-08-22 | 南京荣欣化工有限公司 | Device for preparing n-propyl acetate from carbon dioxide and preparation method thereof |
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