CN205833127U - A kind of ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene - Google Patents
A kind of ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene Download PDFInfo
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- CN205833127U CN205833127U CN201620424183.4U CN201620424183U CN205833127U CN 205833127 U CN205833127 U CN 205833127U CN 201620424183 U CN201620424183 U CN 201620424183U CN 205833127 U CN205833127 U CN 205833127U
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- hexamethylene
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- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 87
- 125000004836 hexamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 title claims abstract description 52
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical group O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 230000003647 oxidation Effects 0.000 claims abstract description 65
- 239000007789 gas Substances 0.000 claims description 91
- 239000007788 liquid Substances 0.000 claims description 52
- 239000007791 liquid phase Substances 0.000 claims description 42
- 238000005406 washing Methods 0.000 claims description 28
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 230000008859 change Effects 0.000 claims description 8
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 7
- 230000003068 static effect Effects 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 abstract description 27
- 239000002994 raw material Substances 0.000 abstract description 22
- 238000000034 method Methods 0.000 abstract description 9
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 230000008569 process Effects 0.000 abstract description 4
- 230000001590 oxidative effect Effects 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract 2
- 230000005587 bubbling Effects 0.000 abstract 1
- 150000001934 cyclohexanes Chemical class 0.000 abstract 1
- 238000002955 isolation Methods 0.000 abstract 1
- 238000003756 stirring Methods 0.000 abstract 1
- 238000005057 refrigeration Methods 0.000 description 19
- 239000000126 substance Substances 0.000 description 12
- 239000000047 product Substances 0.000 description 11
- 239000012071 phase Substances 0.000 description 10
- 238000001816 cooling Methods 0.000 description 8
- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 description 8
- 239000000463 material Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 230000008676 import Effects 0.000 description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 4
- LIKMAJRDDDTEIG-UHFFFAOYSA-N n-hexene Natural products CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 description 4
- 208000035126 Facies Diseases 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000002826 coolant Substances 0.000 description 3
- 230000006837 decompression Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- -1 hexamethylene Alkane Chemical class 0.000 description 3
- 239000012263 liquid product Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 230000008961 swelling Effects 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- 239000001361 adipic acid Substances 0.000 description 2
- 235000011037 adipic acid Nutrition 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000012847 fine chemical Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 229910000851 Alloy steel Inorganic materials 0.000 description 1
- 229920002292 Nylon 6 Polymers 0.000 description 1
- 229920002302 Nylon 6,6 Polymers 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000004703 alkoxides Chemical class 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 239000003429 antifungal agent Substances 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- LLEMOWNGBBNAJR-UHFFFAOYSA-N biphenyl-2-ol Chemical compound OC1=CC=CC=C1C1=CC=CC=C1 LLEMOWNGBBNAJR-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 235000013599 spices Nutrition 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a kind of ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene, this device is made up of feed system, ultra high efficiency tower oxidation reactor R 1 main reactor system and reaction end gas green treatment system.This Cyclohexane Oxidation Unit is using air as oxide isolation, simultaneously using the high-temperature high-voltage reaction tail gas of discharge in oxidizing process as a heat source, enter First Heat Exchanger H 1 and release heat, and be used for heating room temperature hexamethylene raw material by liberated heat, simultaneously using the product overflowed as post bake thermal source, the product overflowed enters the 3rd heat exchanger H 3, again heating hexamethylene raw material.This utility model is compared with traditional tower bubbling oxidation reaction device or stirring autoclave oxidation reaction apparatus, reaction efficiency, yield of Ketohexamethylene are improved, ton Ketohexamethylene product comprehensive energy consumption reduces, comprehensive production cost reduces, and belongs to the green oxidation reaction unit of ultra high efficiency truly.
Description
Technical field
This utility model relates to the device of a kind of oxidizing ethyle alkyl, is specifically related to a kind of be prepared the super of Ketohexamethylene by hexamethylene
Efficient oxidation reaction unit.
Background technology
Ketohexamethylene is important Organic Chemicals, is synthesis of caprolactam, adipic acid and medicine, coating, dyestuff etc.
The important intermediate of fine chemicals, but also be produce spice, rubber antiager, fruit antifungus agent phenylphenol etc. former
Material, it is possible to as the auxiliary agent of fine chemical product, additionally also have the biggest effect in terms of the recovery of printing and plastics.Synthetic fibers
The monomer caprolactam of nylon-6 and nylon-66 and adipic acid are mainly with Ketohexamethylene as raw material production.Current industrial ring
Generally there is the problem that efficiency is low and energy and material consumption is high in the technique of hexane oxidation preparing cyclohexanone.Traditional cyclohexane oxidation
Operation temperature is 160-165 DEG C, and operation pressure is about about 1.2MPa.Low (the 3-of this reaction process not only cyclohexane conversion
5%), response time length, energy consumption high, but also there is the many disadvantage of by-product of Ketohexamethylene poor selectivity, generation.Therefore, send out
Exhibition ultra high efficiency, low energy consumption, the cyclohexane oxidation new technology of low material consumption are the only ways of Ketohexamethylene manufacturing technology.
Utility model content
Prepare the defect of Ketohexamethylene reaction process for solving existing cyclohexane oxidation, this utility model provides a kind of by hexamethylene
Alkane prepares the device and method of the ultra high efficiency oxidation reaction of Ketohexamethylene.This utility model is it is critical that devise ultra high efficiency oxygen
Change reactor R-1 and reaction end gas green processes new system.
One of the purpose of this utility model is to provide a kind of ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene,
Including hexamethylene pans C-1, compressor C-2, gas-liquid separation-surge tank C-3, cold tail gas washing tower C-4, surge tank C-5, surpass
Efficient tower type oxidation reactor R-1, self-priming ultra-fine bubble breaker S-1, heat exchanger H-1, H-2, H-3, cryogenic separator CS-
1, pump and pipeline, described hexamethylene pans C-1 is provided with catalyst inlet the second pipeline 2, bottom hexamethylene pans C-1 with
Ultra high efficiency tower oxidation reactor R-1 bottom is connected by the 6th pipeline 6；Described ultra high efficiency tower oxidation reactor R-1 top
Outlet is connected by the tenth pipeline, the 12nd pipeline with cold tail gas washing tower C-4 bottom, and the tenth pipeline is provided with First Heat Exchanger
H-1, ultra high efficiency tower oxidation reactor R-1 top is provided with liquid-phase reaction product outlet, and this outlet is connected with surge tank C-5, slow
Rush tank C-5 outlet at bottom and the 3rd heat exchanger H-3 connects, top and ultra high efficiency tower oxidation reactor R-1 top exit the tenth
Pipeline 10 is connected；Cyclohexane feed the first pipeline 1 passes sequentially through First Heat Exchanger H-1 and the surge tank that cold tail gas washing tower connects
The 3rd heat exchanger H-3 that C-5 connects finally is connected with hexamethylene pans C-1；Bottom described cold tail gas washing tower C-4 and hexamethylene
Alkane pans C-1 is connected, and top is connected with cryogenic separator CS-1, with cold washing tail gas bottom described cryogenic separator CS-1
Tower C-4 top is connected；A self-priming ultra-fine bubble breaker S-it is provided with inside described ultra high efficiency tower oxidation reactor R-1
1, self-priming ultra-fine bubble breaker S-1 are connected with gas-liquid separation-surge tank C-3 top by the 5th pipeline 5, and this gas-liquid is divided
On-surge tank C-3, connection has air intlet the 4th pipeline 4, and air intlet pipeline is provided with compressor C-2.
Described ultra high efficiency tower oxidation reactor R-1 is internally provided with distributor and gas-liquid distribution baffle plate, described self-priming
Ultra-fine bubble breaker S-1 is arranged on the top of distributor, is fixed on gas-liquid distribution baffle plate, at self-priming ultra-fine bubble breaking
The gas liquid outlet end of device S-1 is provided with ultra-fine bubble sickle.
A circulation liquid phase entrance, liquid phase is had on described ultra high efficiency tower oxidation reactor R-1 every two-layer gas-liquid baffle plate
Ultra high efficiency tower oxidation reactor R-1 is entered with tower wall tangential direction.
Concrete, in described ultra high efficiency tower oxidation reactor R-1, self-priming ultra-fine bubble breaker S-1 is installed
It is distributed baffle plate T-1 with N block gas-liquid ..., T-N, this self-priming ultra-fine bubble breaker S-1 are arranged on the reaction of ultra high efficiency tower oxidation
The bottom of device R-1 and be positioned at the top of distributor, is fixed on gas-liquid baffle plate, and baffle plate is fixed with tower wall, and its percent opening is tower
The 8-16% of sectional area, has circulation liquid phase to input from the tangential direction of tower wall, enters ultra high efficiency between every two-layer gas-liquid baffle plate
Tower oxidation reactor R-1；Self-priming ultra-fine bubble breaker S-1 is by a liquid circulation being arranged on outside reactor R-1
Pump two P-2 provides liquid stream circulation, and by the pipeline composition pipeline loop between coupled reaction device tower body R-1 and S-1, it is gone here and there
Connection installs the heat such as heat exchanger, control valve, effusion meter, matter regulation and control components and parts.Gas-liquid at self-priming ultra-fine bubble breaker S-1 goes out
Mouth end, being provided with aperture is the ultra-fine bubble sickle that 100nm-500 μm porous material is made, and this bubble sickle is by stainless
Steel (titanium material, zirconium material, steel alloy, high Ni-based rustless steel etc.), industrial ceramics or other high-strength high temperature-resistant resistant material are made.
Self-priming ultra-fine bubble breaker S-1 has gas from sucking two kinds of functions of gentle bubble super fine crushing.By self-priming ultra-fine gas
The gas of bubble destroyer S-1, bubble is fractured into ultramicro air bubble (between bubble size distribution substantially 300nm-600 μm), enters
Entering and react bottom reactor R-1, this makes the phase contact area of gas-liquid two-phase in reactor increase several times at least, the most tens of
Times, even more than hundreds of times, it is greatly enhanced gas-liquid mass transfer area and gas-liquid mass transfer rate, thus macroscopic view can be improved unconventionally
Response speed.
Specifically, in the middle part of ultra high efficiency tower oxidation reactor R-1, it is provided with circulation liquid-phase outlet, this exit the 7th pipeline 7
Be provided with pump two P-2, the second condenser F-2 and the second heat exchanger H-2, and with the circulation fluid on ultra high efficiency tower oxidation reactor
Phase entrance is connected, and one of them circulation liquid phase entrance is connected with self-priming ultra-fine bubble breaker S-1；The tower oxygen of described ultra high efficiency
Change and be additionally provided with equipped with the 8th pipeline 8 emptying valve bottom reactor R-1.
On the 6th pipeline 6 being connected with ultra high efficiency tower oxidation reactor R-1 bottom bottom described hexamethylene pans C-1
It is additionally provided with pump one P-1, the first condenser F-1 and static mixer M-1.
Device described in the utility model comprises reaction end gas green simultaneously and processes new system, and it is washed from refrigeration tail gas by one
Wash tower C-4 and a cryogenic separator CS-1 composition, reaction end gas is carried out deep purifying and energy regenerating.Described from refrigeration
Tail gas washing tower C-4, is that the energy of the High Temperature High Pressure tail gas utilizing reactor R-1 top to discharge freezes, then at refrigeration tail
The Organic substance that in gas wash tower C-4, cooled exhaust gas self is carried secretly, including raw material (hexamethylene) and a small amount of product Ketohexamethylene, Hexalin
Deng, make they condensations and collected bottom refrigeration tail gas washing tower C-4, delivering to hexamethylene by delivery pump three P-3 the most again
Alkane pans C-1 enters reaction cycle again.Its principles of science is: the High Temperature High Pressure tail gas that reactor R-1 top is discharged has relatively
High energy (155-160 DEG C, about 1.0MPa), first passes through First Heat Exchanger H-1 preheating ring hexane raw material, makes exhaust temperature
Decline.Tail gas (about about 100 DEG C, 0.5-0.8MPa) after cooling decompression is entered system by the 11st pipeline 11 by through air relief valve
Cold tail gas washing tower C-4, wherein, tail gas drastically swelling heat absorption makes rapid drop in temperature in scrubbing tower C-4, and in tower, temperature may
Being down to 20-30 DEG C, pressure is down to 0.11-0.12MPa now, the Organic substance carried secretly in tail gas, and wherein most is raw material (hexamethylene
Alkane) and a small amount of product Ketohexamethylene, Hexalin etc., condensed in the filler of refrigeration tail gas washing tower C-4 and obtained at the bottom of tower
Collect, thus contained by tail gas pressure can be fully used.Hereafter, the essentially tail gas of normal temperature and pressure enters back into deep cooling and divides
From device CS-1, in cryogenic separator CS-1, tail gas separates again under the coolant deep cooling of about-5 DEG C, the denier of remaining
Organic substance is trapped wherein, and is collected in the bottom tank of CS-1, and it will flow into refrigeration tail gas by overflow control mode
Scrubbing tower C-4 packing layer top.Finally, almost clean reaction air tail gas is vented by the 22nd pipeline 22.
The two of the purpose of this utility model are to provide the method that described device prepares Ketohexamethylene, and as shown in Figure 1, it includes
Three Main Stage:
In the charging stage, first room temperature hexamethylene raw material is heated by the reaction end gas of High Temperature High Pressure at First Heat Exchanger H-1
To about 70 DEG C, the liquid phase gone out by the 24th pipeline 24 overflow by reactor upper side at the 3rd heat exchanger H-3 subsequently
Product continues to be heated to 84-85 DEG C and enters hexamethylene pans C-1, catalyst the most simultaneously by the second pipeline 2 add to
In hexamethylene pans C-1.With raw material pump one P-1 that is connected by the 3rd pipeline 3 bottom hexamethylene pans C-1 to specify
Hexamethylene raw material after flow will heat up delivers to the bottom of ultra high efficiency tower oxidation reactor R-1, the 6th pipe by the 6th pipeline 6
Self controlling valve, effusion meter and static mixer M-1 it is in series with on line 6.
Meanwhile, clean air through compressor C-2 be compressed to 1.2MPa, about 120 DEG C, then through gas-liquid separation-slow
Rush in tank C-3 dried, be connected with self-priming ultra-fine bubble breaker S-1 flange by the 5th pipeline 5.At self-priming ultra-fine gas
In bubble destroyer S-1, air is fractured into bottom ultra-fine bubble entrance ultra high efficiency tower oxidation reactor R-1 and carries out oxidation instead
Should.
In the oxidation reaction stage, after hexamethylene and clean air enter in ultra high efficiency tower oxidation reactor R-1,
Carrying out oxidation reaction under catalyst action, operation temperature is 155-160 DEG C, and operation pressure is 8-10atm.Described ultra high efficiency is tower
The gas-liquid baffle plate T-1 of oxidation reactor R-1 ... T-N is gas-liquid baffle plate, and its percent opening is the 8-16% that tower section is long-pending, every two-layer
Circulation liquid phase is had to input from the tangential direction of tower wall, as shown in Figure 2 between gas-liquid baffle plate.Self-priming ultra-fine bubble breaker
S-1 is arranged on the lower half of ultra high efficiency tower oxidation reactor R-1.In raw material continually enters reactor R-1 with reaction constantly
When carrying out, the liquid level in ultra high efficiency tower oxidation reactor R-1 will gradually rise therewith, and when it, to reach ultra high efficiency tower oxidation anti-
When answering device R-1 upper aqueous phase overfall, the reactant mixture liquid phase of high temperature will flow into surge tank C-by the 24th pipeline 24
5, now, after partially liq vaporization, import the tenth pipeline 10 by the 25th pipeline 25, liquid phase enters the 3rd heat exchanger H-3,
Follow-up workshop section is entered finally by the 9th pipeline 9.
At tail gas treatment stage, the temperature through the tail gas of heat exchanger H-1 is about 100 DEG C, and pressure is 0.5-0.8MPa,
Enter refrigeration tail gas washing tower C-4 through air relief valve, expand wherein and absorb heat, making the operation in refrigeration tail gas washing tower C-4
Rapid drop in temperature.Period, the Organic substance in tail gas is condensed into liquid phase bottom refrigeration tail gas washing tower C-4 by the 13rd
Pipeline 13 flows out, pump three P-3 be transmitted back to hexamethylene pans C-1.Hereafter, remnants have the reaction end gas of micro-content organism to lead to
Crossing the 12nd pipeline 12 and enter cryogenic separator CS-1, remaining Organic substance therein will be condensed further, and by the 19th
Pipeline 19 overflows back refrigeration tail gas washing tower C-4.In this stage to capture rate organic in tail gas more than 99.99% with
On.
Further, the method utilizing said apparatus to prepare Ketohexamethylene, specifically comprise the steps of
Step 1, in hexamethylene pans C-1, add hexamethylene by the first pipeline 1, by the second pipeline 2 to hexamethylene
Adding catalyst in pans C-1, the liquid phase in hexamethylene pans C-1 is entered ultra high efficiency by pump one P-1 by through the 6th pipeline 6
Bottom tower oxidation reactor R-1；
Step 2, by the 4th pipeline 4 air compressed through compressor C-2 it is delivered to gas-liquid separation-surge tank C-3,
Suction ultra-fine bubble breaker S-1 is entered, at self-priming by the 5th pipeline 5 through gas-liquid separation-dried air of surge tank C-3
In formula ultra-fine bubble breaker S-1, air is fractured into bottom ultra-fine bubble entrance ultra high efficiency tower oxidation reactor R-1 and carries out
Oxidation reaction；
Step 3, when the liquid level in ultra high efficiency tower oxidation reactor R-1 exceed middle part circulation liquid-phase outlet time,
Open pump two P-2, respectively by the 15th pipeline the 15, the 16th pipeline the 16, the 17th pipeline the 17, the 18th pipeline 18 by liquid phase
Circulation is delivered to circulate liquid phase entrance and enters ultra high efficiency tower oxidation reactor R-1, and the liquid phase in the 14th pipeline enters self-priming
Formula ultra-fine bubble breaker S-1, the liquid phase in the 15th to the 18th pipeline enters the tower oxygen of ultra high efficiency with tower wall tangential direction
Change reactor R-1；
Step 4, after the pressure in ultra high efficiency tower oxidation reactor R-1 reaches setting value, slowly open tower reaction
The gaseous phase outlet valve at device top, controls exhaust flow, and with operation pressure required in maintaining reaction tower, high temperature tail gas with pressure leads to
Crossing the tenth pipeline 10 and enter First Heat Exchanger H-1, tail gas is expanded to low-temp low-pressure gas by the air relief valve on the 11st pipeline 11
Body enters cold tail gas washing tower C-4, and the organic facies of condensation is transmitted back to hexamethylene pans C-1 by pump three P-3, and gas phase enters deep
Cold separator CS-1, the remaining organic facies of condensation overflows back refrigeration tail gas washing tower C-4, and the remaining organic facies of condensation overflows back system
Cold tail gas washing tower C-4, now gas phase is almost clean reaction air tail gas, can empty；
Step 5, along with the carrying out of oxidation reaction in ultra high efficiency tower oxidation reactor R-1, product is from the tower oxygen of ultra high efficiency
The liquid-phase outlet changing reactor R-1 top overflows, and the High Temperature High Pressure product of spilling enters surge tank C-5, and gas phase passes through the 20th
Five pipelines 25 import ultra high efficiency tower oxidation reactor R-1 top the tenth pipeline 10, and liquid phase is entered by the 26th pipeline 26
3rd heat exchanger H-3, and utilize the heat post bake hexamethylene raw material of liquid phase self, liquid product enters follow-up after cooling
Workshop section；
After step 6, whole device stop, open and empty valve bottom ultra high efficiency tower oxidation reactor R-1, react residual
Stay liquid to pass through the 8th pipeline 8 to be extracted out by pump two P-2.
Described First Heat Exchanger H-1 utilizes the heat hexamethylene raw material of High Temperature High Pressure tail gas self.
Described 3rd heat exchanger H-3 utilizes the heat post bake hexamethylene raw material overflowing liquid product self.
Utilize the pressure energy of tail gas, by air relief valve, realize in refrigeration tail gas washing tower C-4 and cryogenic separator CS-1
The Organic substance carried secretly in tail gas is condensed (deep cooling) trapping.
In above-mentioned reaction new technology, First Heat Exchanger H-1 is to utilize the heat hexamethylene of High Temperature High Pressure tail gas self former
Material.
In above-mentioned reaction new technology, the 3rd heat exchanger H-3 is the heat post bake hexamethylene utilizing and overflowing liquid product self
Alkane raw material.
The purification of the reaction end gas in above-mentioned reaction new technology, is to utilize refrigeration tail gas washing tower C-4 and cryogenic separator
CS-1 realizes the recovery refrigeration of reaction end gas pressure energy, and the Organic substance carried secretly in tail gas condenses (deep cooling) trapping,
Thus realize clean tail gas, improve weight effect more than efficiency thing effect and protection environment.
This utility model is compared to current industrial commonly used high energy consumption, high material-consumption, low rate, the hexamethylene of low yield
Alkoxide preparing cyclohexanone technique, has a following outstanding advantages:
(1) reaction efficiency improves 120-300%；
(2) yield of Ketohexamethylene improves more than 8%；
(3) ton Ketohexamethylene product comprehensive energy consumption reduces by more than 30%, and comprehensive production cost reduces by more than 12%；(4) it is one
Individual super
Efficient green oxidation reaction process.
Accompanying drawing explanation
Fig. 1 is a kind of ultra high efficiency oxidation reaction new technological flow schematic diagram being prepared Ketohexamethylene by hexamethylene.Wherein: C-1
For hexamethylene pans, C-2 is compressor, C-3 be gas-liquid separation-surge tank, C-4 for refrigeration tail gas washing tower, CS-1 is deep
Cold separator, F-1, F-2 be respectively the first condenser, the second condenser, and H-1, H-2, H-3 respectively first, second, third changes
Hot device, M-1 is static mixer, and P-1, P-2, P-3 are respectively pump one, pump two, pump three, and R-1 is the reaction of ultra high efficiency tower oxidation
Device, S-1 is self-priming ultra-fine bubble breaker, and 1-26 is respectively the first to the 26th pipeline.
Fig. 2 is the schematic cross-section that ultra high efficiency tower oxidation reactor R-1 circulating liquid flows to.
Detailed description of the invention
Embodiment 1:
The tower diameter of ultra high efficiency tower oxidation reactor R-1 is 800mm, and tower height is 4.5m, has five layers of gas-liquid baffle plate, gas-liquid
Baffle plate percent opening is 10%, and self-priming ultra-fine bubble breaker S-1 is fixed on ground floor gas-liquid baffle plate central authorities, self-priming ultra-fine
The bottom gas liquid outlet end of bubble breaker S-1, being provided with aperture is the ultra-fine bubble sickle that 100 μm porous materials are made,
Plate spacing between gas-liquid baffle plate is 0.4m, has a circulation liquid-phase outlet below ground floor gas-liquid baffle plate.Rank are started in reaction
Section, is passed through the hexamethylene raw material of 100kg/h in the first pipeline 1, and cyclohexene raw material is through cyclohexene pans C-1 and catalyst
Mixing, is delivered in static mixer M-1 be sufficiently mixed by pump one P-1 by the 3rd pipeline 3, is entered by the 6th pipeline 6 subsequently
The bottom of excess of imports efficient tower type oxidation reactor R-1, being passed through temperature by compressor C-2 in gas-liquid separation-surge tank C-3 is
120 DEG C, pressure be the air of 5atm, air after drying enters self-priming ultra-fine bubble breaker S-1 by the 5th pipeline 5,
Air is made into bottom super broken bubble entrance ultra high efficiency tower oxidation reactor R-1 carrying out oxidation reaction, when the tower oxygen of ultra high efficiency
When liquid level in change reactor R-1 exceedes circulation liquid-phase outlet, opening pump two P-2, liquid phase passes through the 7th pipeline 7 by pump two
P-2 is respectively delivered to self-priming ultra-fine bubble breaker S-1 and liquid phase circulation entrance, and wherein circulation liquid phase is entered with tower wall tangential direction
Enter in tower.Set the operation temperature of ultra high efficiency tower oxidation reactor R-1 as 140 DEG C, pressure as 6atm, when the tower oxygen of ultra high efficiency
After pressure in change reactor R-1 reaches setting value, the gas phase opening ultra high efficiency tower oxidation reactor R-1 top lentamente goes out
Mouth valve, control exhaust flow is 12m3/ h, to maintain the operation pressure in ultra high efficiency tower oxidation reactor R-1, high temperature is high
The tail gas of pressure arrives First Heat Exchanger H-1, and hexamethylene raw material is heated to 100 DEG C, and tail gas passes through the 11st pipeline 11 by reducing pressure
Refrigeration tail gas washing tower C-4, tail gas rapid drop in temperature in drastically swelling heat absorption makes tower in tower, Ta Neiwen is entered after valve decompression
Degree is down to 25 DEG C, and Organic substance is condensed into liquid phase and is transmitted back to hexamethylene pans C-1 by pump three P-3, the tail gas folder of normal temperature and pressure
The Organic substance of a little residual of band enters cryogenic separator CS-1, and tail gas separates again under the coolant deep cooling of-5 DEG C, the pole of residual
Micro-content organism is condensed into liquid phase and overflows back refrigeration tail gas washing tower C-4, and air is discharged.As ultra high efficiency tower oxidation reactor R-
After liquid level in 1 exceedes overfall, opening the valve of overfall, the product of spilling enters slow by the 24th pipeline 24
Rushing tank C-5, the gas phase of reduction vaporization imports the tenth pipeline 10 by the 25th pipeline 25, and liquid phase enters the 3rd heat exchanger H-3
Post bake raw material, is heated to 120 DEG C by hexamethylene, enters follow-up workshop section with afterproduct by the 26th pipeline 26.Finally
In tail gas, organic capture rate reaches more than 99.9%, and tail gas and product pressure can reach 80% with the utilization rate of heat.
Embodiment 2
The tower diameter of ultra high efficiency tower oxidation reactor R-1 is 800mm, and tower height is 4.5m, has five layers of gas-liquid baffle plate, gas-liquid
Baffle plate percent opening is 10%, and self-priming ultra-fine bubble breaker S-1 is fixed on ground floor gas-liquid baffle plate central authorities, self-priming ultra-fine
The bottom gas liquid outlet end of bubble breaker S-1, being provided with aperture is the ultra-fine bubble sickle that 100 μm porous materials are made,
Plate spacing between gas-liquid baffle plate is 0.4m, has a circulation liquid-phase outlet below ground floor gas-liquid baffle plate.Rank are started in reaction
Section, is passed through the hexamethylene raw material of 150kg/h in the first pipeline 1, and cyclohexene raw material is through cyclohexene pans C-1 and catalyst
Mixing, is delivered in static mixer M-1 be sufficiently mixed by pump one P-1 by the 3rd pipeline 3, is entered by the 6th pipeline 6 subsequently
The bottom of excess of imports efficient tower type oxidation reactor R-1, being passed through temperature by compressor C-2 in gas-liquid separation-surge tank C-3 is
120 DEG C, pressure be the air of 5atm, air after drying enters self-priming ultra-fine bubble breaker S-1 by the 5th pipeline 5,
Air is made into bottom super broken bubble entrance ultra high efficiency tower oxidation reactor R-1 carrying out oxidation reaction, when the tower oxygen of ultra high efficiency
When liquid level in change reactor R-1 exceedes circulation liquid-phase outlet, opening pump two P-2, liquid phase passes through the 7th pipeline 7 by pump two
P-2 is respectively delivered to self-priming ultra-fine bubble breaker S-1 and liquid phase circulation entrance, and wherein circulation liquid phase is entered with tower wall tangential direction
Enter in tower.Set the operation temperature of ultra high efficiency tower oxidation reactor R-1 as 160 DEG C, pressure as 7atm, when the tower oxygen of ultra high efficiency
After pressure in change reactor R-1 reaches setting value, the gas phase opening ultra high efficiency tower oxidation reactor R-1 top lentamente goes out
Mouth valve, control exhaust flow is 18m3/ h, to maintain the operation pressure in ultra high efficiency tower oxidation reactor R-1, high temperature is high
The tail gas of pressure arrives First Heat Exchanger H-1, and hexamethylene raw material is heated to 110 DEG C, and tail gas passes through the 11st pipeline 11 by reducing pressure
Refrigeration tail gas washing tower C-4, tail gas rapid drop in temperature in drastically swelling heat absorption makes tower in tower, Ta Neiwen is entered after valve decompression
Degree is down to 25 DEG C, and Organic substance is condensed into liquid phase and is transmitted back to hexamethylene pans C-1 by pump three P-3, the tail gas folder of normal temperature and pressure
The Organic substance of a little residual of band enters cryogenic separator CS-1, and tail gas separates again under the coolant deep cooling of-5 DEG C, the pole of residual
Micro-content organism is condensed into liquid phase and overflows back refrigeration tail gas washing tower C-4, and air is discharged.As ultra high efficiency tower oxidation reactor R-
After liquid level in 1 exceedes overfall, opening the valve of overfall, the product of spilling enters slow by the 24th pipeline 24
Rushing tank C-5, the gas phase of reduction vaporization imports the tenth pipeline 10 by the 25th pipeline 25, and liquid phase enters the 3rd heat exchanger H-3
Post bake raw material, is heated to 125 DEG C by hexamethylene, enters follow-up workshop section with afterproduct by the 26th pipeline 26.Finally
In tail gas, organic capture rate reaches more than 99.9%, and tail gas and product pressure can reach 75% with the utilization rate of heat.
Claims (5)
1. the ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene, it is characterised in that include hexamethylene pans
(C-1), compressor (C-2), gas-liquid separation-surge tank (C-3), cold tail gas washing tower (C-4), surge tank (C-5), ultra high efficiency tower
Formula oxidation reactor (R-1), self-priming ultra-fine bubble breaker (S-1), heat exchanger (H-1, H-2, H-3), cryogenic separator
(CS-1), pump and pipeline, described hexamethylene pans (C-1) are provided with catalyst inlet the second pipeline (2), hexamethylene pans
(C-1) bottom is connected by the 6th pipeline (6) with ultra high efficiency tower oxidation reactor (R-1) bottom；The tower oxygen of described ultra high efficiency
Change reactor (R-1) top exit with cold tail gas washing tower (C-4) bottom by the tenth pipeline (10) and the 11st pipeline (11)
Connecting, the tenth pipeline (10) is provided with First Heat Exchanger (H-1), and ultra high efficiency tower oxidation reactor (R-1) top is provided with liquid phase
Reacting product outlet, this outlet is connected with surge tank (C-5), and surge tank (C-5) outlet at bottom and the 3rd heat exchanger (H-3) are even
Connecing, top is connected with ultra high efficiency tower oxidation reactor (R-1) top the tenth pipeline (10)；Cyclohexane feed the first pipeline (1)
Pass sequentially through First Heat Exchanger (H-1) that cold tail gas washing tower connects and the 3rd heat exchanger (H-3) that connects of surge tank (C-5)
It is connected with hexamethylene pans (C-1) eventually；Described cold tail gas washing tower (C-4) bottom is connected with hexamethylene pans (C-1), top
Portion is connected with cryogenic separator (CS-1), and described cryogenic separator (CS-1) bottom is connected with cold tail gas washing tower (C-4) top；
Described self-priming ultra-fine bubble breaker (S-1) is positioned at the lower inside of ultra high efficiency tower oxidation reactor (R-1), and this is self-priming
Ultra-fine bubble breaker (S-1) is connected with gas-liquid separation-surge tank (C-3) top by the 5th pipeline (5), and this gas-liquid separation-
The upper connection of surge tank (C-3) has air intlet the 4th pipeline (4), and air intlet pipeline is provided with compressor (C-2).
A kind of ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene the most according to claim 1, its feature exists
In, described ultra high efficiency tower oxidation reactor (R-1) is internally provided with distributor and gas-liquid distribution baffle plate, described self-priming ultra-fine
Bubble breaker (S-1) is arranged on the top of distributor, is fixed on gas-liquid distribution baffle plate, at self-priming ultra-fine bubble breaker
(S-1) gas liquid outlet end is provided with ultra-fine bubble sickle.
A kind of ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene the most according to claim 2, its feature exists
In, the every two-layer gas-liquid baffle plate of described ultra high efficiency tower oxidation reactor (R-1) has a circulation liquid phase entrance, liquid phase is with tower
Wall tangential direction enters ultra high efficiency tower oxidation reactor (R-1).
A kind of ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene the most according to claim 3, its feature exists
In, in described device, ultra high efficiency tower oxidation reactor (R-1) middle part is provided with circulation liquid-phase outlet, this exit the 7th pipeline
(7) be provided with pump two (P-2), the second condenser (F-2) and the second heat exchanger (H-2), and with ultra high efficiency tower oxidation reactor
On circulation liquid phase entrance be connected, one of them circulation liquid phase entrance be connected with self-priming ultra-fine bubble breaker (S-1)；Described
Ultra high efficiency tower oxidation reactor (R-1) bottom is additionally provided with equipped with the 8th pipeline (8) emptying valve.
A kind of ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene the most according to claim 1, its feature exists
In, the 6th pipe that described device cyclohexane pans (C-1) bottom is connected with ultra high efficiency tower oxidation reactor (R-1) bottom
Pump one (P-1), the first condenser (F-1) and static mixer (M-1) it is additionally provided with on road (6).
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| CN201620424183.4U CN205833127U (en) | 2016-05-11 | 2016-05-11 | A kind of ultra high efficiency oxidation reaction apparatus being prepared Ketohexamethylene by hexamethylene |
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| CN105797654A (en) * | 2016-05-11 | 2016-07-27 | 南京大学 | Super-efficient oxidation reaction device and method for preparing cyclohexanone from cyclohexane |
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| CN112174790A (en) * | 2019-07-04 | 2021-01-05 | 南京延长反应技术研究院有限公司 | Reinforcing system and process for producing cyclohexanone by cyclohexane oxidation method |
| DE212020000665U1 (en) | 2020-05-14 | 2022-04-26 | Nanjing Yanchang Reaction Technology Research Institute Co. Ltd | Enhanced reaction system for producing cyclohexanone by selective hydrogenation of benzene |
| WO2021253310A1 (en) | 2020-06-17 | 2021-12-23 | 南京延长反应技术研究院有限公司 | MICRO-INTERFACE STRENGTHENING REACTION SYSTEM AND METHOD FOR PREPARING POLY-α-OLEFIN |
| WO2022011867A1 (en) | 2020-07-16 | 2022-01-20 | 南京延长反应技术研究院有限公司 | Micro-interface reaction system and method for diesel hydrogenation |
| DE212020000670U1 (en) | 2020-07-16 | 2022-04-25 | Nanjing Yanchang Reaction Technology Research Institute Co. Ltd | Coal-to-Ethanol Reaction System |
| WO2022032869A1 (en) * | 2020-08-11 | 2022-02-17 | 南京延长反应技术研究院有限公司 | Micro-interface strengthening system and method for preparing sodium n-methyl taurate |
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