CN104262116A - MTBE deep desulfurization device and method thereof - Google Patents
MTBE deep desulfurization device and method thereof Download PDFInfo
- Publication number
- CN104262116A CN104262116A CN201410281033.8A CN201410281033A CN104262116A CN 104262116 A CN104262116 A CN 104262116A CN 201410281033 A CN201410281033 A CN 201410281033A CN 104262116 A CN104262116 A CN 104262116A
- Authority
- CN
- China
- Prior art keywords
- tower
- mtbe
- distillation tower
- discharge port
- static mixer
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 17
- 230000023556 desulfurization Effects 0.000 title abstract description 6
- 238000004821 distillation Methods 0.000 claims abstract description 63
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 38
- 230000003068 static effect Effects 0.000 claims abstract description 25
- 238000002347 injection Methods 0.000 claims abstract description 12
- 239000007924 injection Substances 0.000 claims abstract description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 39
- 235000003599 food sweetener Nutrition 0.000 claims description 38
- 239000000047 product Substances 0.000 claims description 38
- 239000003765 sweetening agent Substances 0.000 claims description 38
- 229910052717 sulfur Inorganic materials 0.000 claims description 25
- 239000011593 sulfur Substances 0.000 claims description 25
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 24
- 229910052799 carbon Inorganic materials 0.000 claims description 24
- 239000012071 phase Substances 0.000 claims description 19
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 14
- 150000001875 compounds Chemical class 0.000 claims description 10
- 238000002156 mixing Methods 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 9
- 239000002699 waste material Substances 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 8
- 230000003009 desulfurizing effect Effects 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 5
- 239000000470 constituent Substances 0.000 claims description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 3
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 3
- 230000000536 complexating effect Effects 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 239000004571 lime Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 239000005864 Sulphur Substances 0.000 abstract description 15
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000007788 liquid Substances 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 20
- 238000005516 engineering process Methods 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 8
- 239000003915 liquefied petroleum gas Substances 0.000 description 6
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 4
- 150000003568 thioethers Chemical class 0.000 description 4
- 238000005261 decarburization Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000003112 inhibitor Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- BWGNESOTFCXPMA-UHFFFAOYSA-N Dihydrogen disulfide Chemical compound SS BWGNESOTFCXPMA-UHFFFAOYSA-N 0.000 description 1
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 1
- MRRWPCWICIRLDJ-UHFFFAOYSA-N [S].CCO Chemical compound [S].CCO MRRWPCWICIRLDJ-UHFFFAOYSA-N 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 238000010668 complexation reaction Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000000895 extractive distillation Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
- C07C41/36—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to an MTBE deep desulfurization device. The MTBE deep desulfurization device comprises a static mixer, a distillation column, a condenser, a circulating pump, an injection pump, a reboiler and a waste-liquid storage tank. The static mixer is connected to a feeding port at the middle part of the distillation column. The circulating pump is connected between the static mixer and a circulating port at the lower part of the distillation column. The static mixer is also connected to the injection pump. The bottom of the distillation column is connected to the waste-liquid storage tank. The lower part of the distillation column is connected to the reboiler. The bottom of the distillation column is provided with a coalescent pack. The middle and lower part of the coalescent pack is provided with an MTBE product outlet. A process of the MTBE deep desulfurization device is simple. By simple reconstruction of the distillation column, the total sulphur content of MTBE can be reduced from hundreds even thousands ppm to less than 10 ppm, and the yield of an MTBE product is increased from 80% to more than 99%, thus achieving low energy consumption, low cost and high benefit.
Description
Technical field
The present invention relates to the deep removal field of MTBE medium sulphide content, particularly relate to a kind of MTBE deep desulfuration devices and methods therefor.
Background technology
Along with the raising day by day of national requirements for environmental protection, motor spirit quality standard is constantly upgraded, more and more stricter to the restriction of content of sulfur in gasoline, the sulphur content of state IV motor spirit requires to be less than 50ppm, state V requires to be less than 10ppm, National Standards Commission proposed from January, 2018, nationwide by supply country V gasoline.
Methyl tertiary butyl ether (MTBE) is with its high-octane rating and good blending performance, and become the main blend component improving petrol and diesel oil octane value and add oxygenatedchemicals, blending ratio is generally 8%-15%.At present, the sulphur content of the MTBE product being raw material production with catalysis and coker production fluid liquefied oil gas mixed c 4 changes greatly, and is generally 100-500ppm, have up to 2000-3000ppm.During producing country's V motor spirit, even if adopt S-Zorb technology to make catalytic gasoline sulfur nutrient be reduced to below 10ppm, still need to reduce sulphur content in MTBE, the sulphur content index of state V motor spirit could be met.Along with closing on of state V motor spirit standard implementation, more and more urgent to the demand of low-sulfur MTBE production technology.
MTBE raw materials for production are the liquefied petroleum gas (LPG) containing iso-butylene, and liquefied petroleum gas (LPG) institute sulfur compound is mainly the organic sulfides such as hydrogen sulfide, methyl alcohol sulphur, ethanol sulphur, thioether and a small amount of disulphide, also has individual device to contain thiophenic sulfur.Liquefied petroleum gas (LPG) washes the hydrogen sulfide and mercaptan that can remove the overwhelming majority with alkaline cleaner through amine, but thioether, disulphide and thiophenic sulfur almost cannot remove, these sulphur cause MTBE product total sulfur higher the most at last, in addition, traditional liquid gas sweetening Merox technique and other technologies, cannot be separated owing to generating disulphide in alkali liquor oxidized regenerative process, even if adopt solvent oil back suction to carry remove dioxide, still have a small amount of disulphide to be stripped in liquefied refinery gas, this is also the major reason causing MTBE total sulfur high.
For reducing MTBE total sulfur content, at present domestic with or the technology developed have:
Sources controlling, adopt advanced technologies to remove mercaptan and neutral sulphur in liquefied gas as far as possible, from Sources controlling MTBE total sulfur, but in this process, neutral sulphur not easily removes, and causes follow-up MTBE total sulfur high.
Carbon four desulfurization, adopt alkali cleaning and similar molecular sieve to absorb combination process and divide rear carbon four to carry out fine de-sulfur to gas, because carbon four only accounts for the 20-40% of liquefied gas total amount, it is still higher that carbon four refines cost, and regenerating molecular sieve complicated operation, labour intensity are large.
Separation of carbon five, sulfur speciation in carbon four is utilized to be mainly the larger Macromolecule mercaptan of molecular weight, disulfide and micro-thiophenic sulfur, the carbon five in carbon four is removed with decarburization five tower, macromole sulphur is dissolved in carbon five, realize the object of carbon four desulfurization, but this technology is more applicable to only having the situation of macromole Sulfur, to carbon four containing low molecule mercaptan, the situation then less effective of thioether, thus there is the different device adopting same decarburization five tower, MTBE still reaches the situation of tens ppm, simultaneously, carbon four decarburization five pairs of rectifying tower fractionation precision are very high, energy consumption is larger, cost is higher.
Liquefied gas deep desulfuration and MTBE extractive distillation, transform liquid gas sweetening system, increases by three mixed regeneration towers, back suctions and carry the equipment such as tunica fibrosa, reduces liquefied refinery gas sulphur content; At the newly-increased extraction distillation column of MTBE device, by interpolation antigum inhibitor, the heavy constituent sulphur in MTBE is carried out distillation extraction to remove, domesticly at present mainly use this technique, but this technology investment is relatively large, and when the higher antigum inhibitor usage quantity of total sulfur in MTBE will be larger, working cost and interpolation auxiliary agent expense are actually above 150 yuan/ton, and the yield of MTBE is about about 99% simultaneously, and this technique still needs to improve.
Summary of the invention
For the present situation of above-mentioned prior art, it is good that technical problem to be solved by this invention is to provide a kind of sweetening effectiveness, and sweetening agent consumption is few, and energy consumption is low, and cost is few, the MTBE deep desulfuration devices and methods therefor of energy-conserving and environment-protective.
The present invention solves the problems of the technologies described above adopted technical scheme: a kind of MTBE deep desulfuration device, comprise static mixer, distillation tower, condenser, recycle pump, injection pump, reboiler and waste tank, described static mixer is connected with the opening for feed in the middle part of distillation tower, recycle pump is connected with between the circulation port of this static mixer and distillation tower bottom, static mixer is also connected with injection pump, the bottom of described distillation tower is connected with waste tank, the bottom of distillation tower is connected with reboiler, the bottom of described distillation tower is provided with coalescent pack, the middle and lower part of distillation tower is provided with MTBE outlet for product, tower bottom installs coalescent pack, to containing desulfurizing agent of sulfur, there is certain coalescence effect, be convenient to the complex compound of separate sulfur compound, improve the yield of MTBE product.
Further, described discharge port comprises the first discharge port, second discharge port and the 3rd discharge port, gas phase collection tube is stretched in being equipped with in this discharge port, described first discharge port, second discharge port, it is relative that the 3rd discharge port detects mouth with the thermopair in distillation tower respectively, can improve the yield of MTBE product.
Further, the top of stretching gas phase collection tube in described is provided with column plate, and this interior pipe portion of stretching gas phase collection tube cuts lower half circle, can prevent dirty liquid phase from going out tower with MTBE product.
Further, the junction of described reboiler and distillation tower is 1000-2000mm to the distance of tower bottom, rich desulfurizing agent of sulfur can be avoided to be mixed into yield that reboiler affects MTBE product.
Further, described recycle pump and distillation tower, static mixer form sweetening agent circular route, effectively realize the recycle of sweetening agent, make full use of sweetening agent, cost-saving.
A kind of MTBE process for deep desulphurization, comprises the following steps:
A, mixing raw material, fresh sweetening agent enters mixture Homogeneous phase mixing after static mixer and etherificate through injection pump, then distillation tower is entered from opening for feed in the middle part of distillation tower, material component containing three kinds of different initial boiling points in distillation tower, is respectively carbon four and methanol azeotrope, MTBE product, the complex compound of sweetening agent and sulfide, control tower top temperature 55-65 DEG C, column bottom temperature 135-145 DEG C, tower sensitive spot temperature 115-125 DEG C;
B, distillation, after mixture enters distillation tower, carbon four and methanol azeotrope and MTBE product are distilled as gas phase is walked toward tower top, and enter rectifying section, sulfide complexing, in sweetening agent, is walked with liquid phase after entering tower, entered stripping section at the bottom of tower;
C, rectifying, in rectifying, MTBE product is all condensed into liquid phase, walk at the bottom of tower, enter stripping section, the condenser of tower top makes carbon four and methanol azeotrope partial condensation, this part lime set returns at the bottom of tower as phegma, and all the other carbon four and methanol azeotrope distillate tower top as distillate and collect;
D, carry and heating up in a steamer, carrying in the process of heating up in a steamer, MTBE product is all vaporized, and distillate from the discharge port of distillation tower and collect, reboiler at the bottom of tower makes the complex compound components vaporize of sweetening agent and sulfide, and gas phase rises along tower, and the complex compound of remaining most heavy constituent sweetening agent and sulfide is as bottom product;
E, bottom product reclaim, and bottom product is through coalescent pack, and rich desulfurizing agent of sulfur is wherein discharged at the bottom of tower, and collect by waste tank, and remaining effective sweetening agent enters static mixer mixing from the circulation port of distillation tower again through recycle pump.
Further, fresh sweetening agent in described step a is DDA-II, this sweetening agent sweetening effectiveness is good, can ensure that MTBE total sulfur is reduced to below 10ppm from hundreds of even thousands of ppm, and doctor solution consumption is few, according to variant production sulphur content flexible sweetening agent addition, production cost can be reduced.
Compared with prior art, the invention has the advantages that: present invention process is simple, by simply transforming distillation tower, coalescent pack is set up at tower bottom, discharge port being located at distillation tower middle and lower part and thermopair, to detect mouth relative, and the pipe portion of stretching gas phase collection tube in discharge port is cut lower half circle, prevent dirty liquid phase from going out tower with MTBE product, the feeding line of distillation tower to be annotated a small amount of efficient desulfurizing agent, can from MTBE product, Separation by Complexation be out by sulfide, thus MTBE total sulfur content is removed to below 10ppm from hundreds of even thousands of ppm, MTBE product yield is brought up to more than 99% by 80%, realize less energy-consumption, low cost, high benefit, in addition, the setting of recycle pump, realize sweetening agent recycle, reduce the consumption of sweetening agent, non-secondary pollution thing discharge of the present invention, energy-conserving and environment-protective are efficient again, accord with the demands of the market, be applicable to large-scale promotion.
Accompanying drawing explanation
Fig. 1 is structure drawing of device of the present invention;
Fig. 2 is MTBE outlet for product structure iron of the present invention.
Embodiment
Below by embodiment, the present invention is described in further detail, and following examples are explanation of the invention and the present invention is not limited to following examples.
As shown in Figure 1-2, a kind of MTBE deep desulfuration device, comprise static mixer 2, distillation tower 1, condenser 3, recycle pump 6, injection pump 7, reboiler 4 and waste tank 5, described static mixer 2 is connected with the opening for feed in the middle part of distillation tower 1, recycle pump 6 is connected with between the circulation port of this static mixer 2 and distillation tower 1 bottom, static mixer 2 is also connected with injection pump 7, the bottom of described distillation tower 1 is connected with waste tank 5, the bottom of distillation tower 1 is connected with reboiler 4, the junction of this reboiler 4 and distillation tower 1 is 1000-2000mm to the distance of tower bottom, rich desulfurizing agent of sulfur can be avoided to be mixed into yield that reboiler 4 affects MTBE product, the bottom of described distillation tower 1 is provided with coalescent pack 8, the middle and lower part of distillation tower 1 is provided with MTBE outlet for product, this discharge port comprises the first discharge port 9, second discharge port 10 and the 3rd discharge port 11, gas phase collection tube 12 is stretched in being equipped with in this discharge port, this interior top of stretching gas phase collection tube 12 is provided with column plate 13, this interior pipe portion of stretching gas phase collection tube 12 cuts lower half circle, can prevent dirty liquid phase from going out tower with MTBE product, described first discharge port 9, second discharge port 10, it is relative that 3rd discharge port 11 detects mouth 14 with the thermopair in distillation tower 1 respectively, the yield of MTBE product can be improved, described recycle pump 6 and distillation tower 1, static mixer 2 forms sweetening agent circular route, effectively realize the recycle of sweetening agent, make full use of sweetening agent, cost-saving, in addition, according to MTBE sulphur content, injection pump 7 can supplement fresh sweetening agent by continuous and quantitative, thus ensure the purity of MTBE product.
A kind of MTBE process for deep desulphurization, comprises the following steps:
A, mixing raw material, fresh sweetening agent enters mixture Homogeneous phase mixing after static mixer 2 and etherificate through injection pump 7, then distillation tower 1 is entered from opening for feed in the middle part of distillation tower 1, material component containing three kinds of different initial boiling points in distillation tower 1, is respectively carbon four and methanol azeotrope, MTBE product, the complex compound of sweetening agent and sulfide, control tower top temperature 60 C, column bottom temperature 135 DEG C, tower sensitive spot temperature 120 DEG C;
B, distillation, after mixture enters distillation tower 1, carbon four and methanol azeotrope and MTBE product are distilled as gas phase is walked toward tower top, and enter rectifying section, sulfide complexing, in sweetening agent, is walked with liquid phase after entering tower, entered stripping section at the bottom of tower;
C, rectifying, in rectifying, MTBE product is all condensed into liquid phase, walk at the bottom of tower, enter stripping section, the condenser 3 of tower top makes carbon four and methanol azeotrope partial condensation, this part lime set returns at the bottom of tower as phegma, and all the other carbon four and methanol azeotrope distillate tower top as distillate and collect;
D, carry and heating up in a steamer, carrying in the process of heating up in a steamer, MTBE product is all vaporized, and distillate from the discharge port of distillation tower 1 and collect, reboiler 4 at the bottom of tower makes the complex compound components vaporize of sweetening agent and sulfide, and gas phase rises along tower, and the complex compound of remaining most heavy constituent sweetening agent and sulfide is as bottom product;
E, bottom product reclaim, and bottom product is through coalescent pack 8, and rich desulfurizing agent of sulfur is wherein discharged at the bottom of tower, and collects by waste tank 5, and remaining effective sweetening agent again enters static mixer 2 from the circulation port of distillation tower 1 through recycle pump 6 and mixes.
Wherein, the fresh sweetening agent in described step a is DDA-II, and this sweetening agent sweetening effectiveness is good, can ensure that MTBE total sulfur is reduced to below 10ppm from hundreds of even thousands of ppm, and doctor solution consumption is few, can according to variant production sulphur content flexible sweetening agent addition, reduce production cost, in addition, in sweetening process, sweetening agent can recycle, realize making full use of of sweetening agent, for rich desulfurizing agent of sulfur recoverable, non-secondary pollution discharges, energy-conservation environmental protection again.
Last it is noted that above embodiment is only in order to illustrate technical scheme of the present invention, be not intended to limit; Although with reference to previous embodiment to invention has been detailed description, it will be understood by those of skill in the art that it still can be modified to the technical scheme described in foregoing embodiments, or wherein portion of techniques feature is replaced on an equal basis; And these amendments or replacement, do not make the essence of appropriate technical solution depart from spirit and the scope of various embodiments of the present invention technical scheme.
Claims (7)
1. a MTBE deep desulfuration device, comprise static mixer (2), distillation tower (1), condenser (3), recycle pump (6), injection pump (7), reboiler (4) and waste tank (5), it is characterized in that, described static mixer (2) is connected with the opening for feed at distillation tower (1) middle part, recycle pump (6) is connected with between the circulation port of this static mixer (2) and distillation tower (1) bottom, static mixer (2) is also connected with injection pump (7), the bottom of described distillation tower (1) is connected with waste tank (5), the bottom of distillation tower (1) is connected with reboiler (4), the bottom of described distillation tower (1) is provided with coalescent pack (8), the middle and lower part of distillation tower (1) is provided with MTBE outlet for product.
2. a kind of MTBE deep desulfuration device according to claim 1, it is characterized in that, described discharge port comprises the first discharge port (9), second discharge port (10) and the 3rd discharge port (11), gas phase collection tube (12) is stretched in being equipped with in this discharge port, described first discharge port (9), second discharge port (10), it is relative that the 3rd discharge port (11) detects mouth (14) with the thermopair in distillation tower (1) respectively.
3. a kind of MTBE deep desulfuration device according to claim 2, is characterized in that, the top of stretching gas phase collection tube (12) in described is provided with column plate (13), and this interior pipe portion of stretching gas phase collection tube (12) cuts lower half circle.
4. a kind of MTBE deep desulfuration device according to claim 1, is characterized in that, the junction of described reboiler (4) and distillation tower (1) is 1000-2000mm to the distance of tower bottom.
5. a kind of MTBE deep desulfuration device according to claim 1, is characterized in that, described recycle pump (6) and distillation tower (1), static mixer (2) form sweetening agent circular route.
6. a MTBE process for deep desulphurization, is characterized in that, comprises the following steps:
A, mixing raw material, fresh sweetening agent enters mixture Homogeneous phase mixing after static mixer (2) and etherificate through injection pump (7), then distillation tower (1) is entered from distillation tower (1) middle part opening for feed, material component containing three kinds of different initial boiling points in distillation tower (1), be respectively carbon four and methanol azeotrope, MTBE product, the complex compound of sweetening agent and sulfide, control tower top temperature 55-65 DEG C, column bottom temperature 135-145 DEG C, tower sensitive spot temperature 115-125 DEG C;
B, distillation, after mixture enters distillation tower (1), carbon four and methanol azeotrope and MTBE product are distilled as gas phase is walked toward tower top, and enter rectifying section, sulfide complexing, in sweetening agent, is walked with liquid phase after entering tower, entered stripping section at the bottom of tower;
C, rectifying, in rectifying, MTBE product is all condensed into liquid phase, walk at the bottom of tower, enter stripping section, the condenser (3) of tower top makes carbon four and methanol azeotrope partial condensation, and this part lime set returns at the bottom of tower as phegma, and all the other carbon four and methanol azeotrope distillate tower top as distillate and collect;
D, carry and heating up in a steamer, carrying in the process of heating up in a steamer, MTBE product is all vaporized, and distillate from the discharge port of distillation tower (1) and collect, reboiler (4) at the bottom of tower makes the complex compound components vaporize of sweetening agent and sulfide, gas phase rises along tower, and the complex compound of remaining most heavy constituent sweetening agent and sulfide is as bottom product;
E, bottom product reclaim, bottom product is through coalescent pack (8), rich desulfurizing agent of sulfur is wherein discharged at the bottom of tower, and collect by waste tank (5), remaining effective sweetening agent enters static mixer (2) mixing from the circulation port of distillation tower (1) again through recycle pump (6).
7. a kind of MTBE process for deep desulphurization according to claim 6, is characterized in that, the fresh sweetening agent in described step a is DDA-II.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410281033.8A CN104262116A (en) | 2014-06-23 | 2014-06-23 | MTBE deep desulfurization device and method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410281033.8A CN104262116A (en) | 2014-06-23 | 2014-06-23 | MTBE deep desulfurization device and method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104262116A true CN104262116A (en) | 2015-01-07 |
Family
ID=52153737
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410281033.8A Pending CN104262116A (en) | 2014-06-23 | 2014-06-23 | MTBE deep desulfurization device and method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104262116A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106316799A (en) * | 2015-07-09 | 2017-01-11 | 上海纳科助剂有限公司 | Ultralow-sulfur methyl tert-butyl ether production device |
| CN108070416A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of liquefied petroleum gas process for adsorption desulfuration |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102219653A (en) * | 2011-04-28 | 2011-10-19 | 山东东明石化集团有限公司 | Method for producing low-sulfur methyl tert-butyl ether product |
| CN102617297A (en) * | 2012-01-13 | 2012-08-01 | 宁波中一石化科技有限公司 | Device and method for removing disulfide from methyl tertiary butyl ether (MTBE) |
| CN103333056A (en) * | 2013-07-17 | 2013-10-02 | 凯瑞化工股份有限公司 | Method and device for deeply removing sulfide in MTBE |
| CN103360221A (en) * | 2013-07-17 | 2013-10-23 | 凯瑞化工股份有限公司 | Method for deeply removing sulfides in MTBE |
| CN203923059U (en) * | 2014-06-20 | 2014-11-05 | 贺立明 | A kind of MTBE deep desulfuration device |
-
2014
- 2014-06-23 CN CN201410281033.8A patent/CN104262116A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102219653A (en) * | 2011-04-28 | 2011-10-19 | 山东东明石化集团有限公司 | Method for producing low-sulfur methyl tert-butyl ether product |
| CN102617297A (en) * | 2012-01-13 | 2012-08-01 | 宁波中一石化科技有限公司 | Device and method for removing disulfide from methyl tertiary butyl ether (MTBE) |
| CN103333056A (en) * | 2013-07-17 | 2013-10-02 | 凯瑞化工股份有限公司 | Method and device for deeply removing sulfide in MTBE |
| CN103360221A (en) * | 2013-07-17 | 2013-10-23 | 凯瑞化工股份有限公司 | Method for deeply removing sulfides in MTBE |
| CN203923059U (en) * | 2014-06-20 | 2014-11-05 | 贺立明 | A kind of MTBE deep desulfuration device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106316799A (en) * | 2015-07-09 | 2017-01-11 | 上海纳科助剂有限公司 | Ultralow-sulfur methyl tert-butyl ether production device |
| CN108070416A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of liquefied petroleum gas process for adsorption desulfuration |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101376842B (en) | Method for reducing sulfur content in gasoline | |
| CN103555359B (en) | Deep desulfurization method for catalytically cracked gasoline | |
| CN205676426U (en) | A kind of device of liquid hydrocarbon fine de-sulfur | |
| CN104694160B (en) | Combined method for light gasoline alkaline washing desulfurization | |
| CN101649221A (en) | Method for producing reforming raw material from gasoline light and medium fractions | |
| CN104829436A (en) | Device and method for deeply removing organic sulphides in methyl tertiary butyl ether (MTBE) | |
| CN102617297B (en) | Device and method for removing disulfide from methyl tertiary butyl ether (MTBE) | |
| CN103922900A (en) | Method for removing sulfide in methyl tertiary butyl ether through double-solvent extractive distillation | |
| CN103911177B (en) | A kind of saturated liquid hydrocarbon deep desulfurization method | |
| CN105777500A (en) | Extraction anti-gum agent for MTBE desulfurization | |
| CN1137967C (en) | Method for separating hydrocarbon hydrocracking products | |
| CN103184071B (en) | Gasoline desulfurization method | |
| CN104262116A (en) | MTBE deep desulfurization device and method thereof | |
| CN101210199B (en) | Method for reducing sulfur content in gasoline | |
| CN1142258C (en) | Process for removing sulfide from gasoline fraction by solvent extraction | |
| CN103641693A (en) | Low-energy-consumption MTBE (methyl tert-butyl ether) production method | |
| CN203923059U (en) | A kind of MTBE deep desulfuration device | |
| CN203530179U (en) | MTBE (Methyl Tert Butyl Ether) deep desulfurization device | |
| CN106278834B (en) | A kind of green MTBE deep desulfuration purifications agent and its in removing methyl tertiary butyl ether(MTBE) sulfide application | |
| CN205501162U (en) | Novel desulfurization of MTBE degree of depth device | |
| CN204723789U (en) | A kind of MTBE deep desulfuration device | |
| CN108018066A (en) | A kind of method of the deep desulfuration containing sulfur feedstock | |
| CN103756721B (en) | A kind of extraction-washing-hydrogenation combination technique producing low-sulphur oil | |
| CN103740407B (en) | Alkali cleaning-extraction-washing-hydrogenation combined process for producing low-sulfur-content gasoline | |
| CN103740405B (en) | Alkali cleaning-extraction-hydrogenation combined process for producing low-sulfur-content gasoline |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| CB03 | Change of inventor or designer information |
Inventor after: He Liming Inventor after: Xu Zhenhua Inventor before: He Liming Inventor before: Xu Zhenhua Inventor before: Wang Shifa |
|
| COR | Change of bibliographic data | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20150916 Address after: 315000 Zhejiang Province, Ningbo high tech Zone Jinghua Road No. 188 Building 2 room 852 Applicant after: NINGBO ZHANGFU ENERGY TECHNOLOGY Co.,Ltd. Address before: 315000 wax surgery group 11, Qixing village, Liling Town, Zhejiang, China Applicant before: He Liming |
|
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 315000, Zhejiang Province, Ningbo province hi tech Zone, 1558 Jiangnan Road, Zhejiang Province, room 1105, science and Technology Park, Zhejiang Applicant after: NINGBO ZHANGFU ENERGY TECHNOLOGY Co.,Ltd. Address before: 315000 Zhejiang Province, Ningbo high tech Zone Jinghua Road No. 188 Building 2 room 852 Applicant before: NINGBO ZHANGFU ENERGY TECHNOLOGY Co.,Ltd. |
|
| CB02 | Change of applicant information | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20150107 |
|
| WD01 | Invention patent application deemed withdrawn after publication |