CN105272832A - Method for removing sulfides in methyl tert-butyl ether through catalytic distillation and adsorption - Google Patents
Method for removing sulfides in methyl tert-butyl ether through catalytic distillation and adsorption Download PDFInfo
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- CN105272832A CN105272832A CN201410248147.2A CN201410248147A CN105272832A CN 105272832 A CN105272832 A CN 105272832A CN 201410248147 A CN201410248147 A CN 201410248147A CN 105272832 A CN105272832 A CN 105272832A
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- butyl ether
- tertiary butyl
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Abstract
The invention relates to a method for removing sulfides in methyl tert-butyl ether, and concretely relates to a method for removing sulfides in methyl tert-butyl ether through catalytic distillation and adsorption. The method comprises the following steps: carrying out catalytic rectification on light mercaptan in methyl tert-butyl ether to convert the light mercaptan under the action of a catalyst into heavy sulfur, separating the heavy sulfur and methyl tert-butyl ether, allowing the separated methyl tert-butyl ether to enter an adsorption tower, and adsorbing methyl tert-butyl ether under the action of an adsorbent to remove light sulfur in order to obtain low-sulfur methyl tert-butyl ether. Compared with the prior art, the method has the advantages of simple flow, low investment cost, and suitableness for industrial production, and allows the total sulfur content of methyl tert-butyl ether to be reduced to 2ppm or below in order to make the obtained methyl tert-butyl ether meet high-grade gasoline blending and subsequent advanced processing utilization demands.
Description
Technical field
The present invention relates to the method removing methyl tertiary butyl ether medium sulphide content, be specifically related to a kind of method being added adsorbing and removing methyl tertiary butyl ether medium sulphide content by catalytic distillation.
Background technology
Along with continuing to increase of vehicle guaranteeding organic quantity, automotive emission is one of main source becoming urban air pollution, and motor spirit quality standard is constantly upgraded, more and more stricter to the restriction of content of sulfur in gasoline.Hydrogen addition technology must be used to make the sulphur content of catalytic gasoline be reduced to certain numerical value when producing high-grade gasoline, the requirement of mediation high-grade gasoline could be met, and the sulphur content reducing catalytic gasoline will inevitably cause the decline of octane value, methyl tertiary butyl ether is as vapour oil additives (general addition is 8% ~ 15%), be mainly used in regulating the octane value of gasoline, therefore directly to affect quality of gasoline up to standard for the sulphur content of methyl tertiary butyl ether.It is complicated that current petroleum chemical enterprise produces the raw materials used source of methyl tertiary butyl ether, and in material carbon four, sulphur content is higher, causes methyl tert-butyl ether product medium sulphide content content more.According to statistics, in major part petrochemical industry producer methyl tert-butyl ether product, sulphur content is higher than 200ppm, quality product can not be met the need of market, product price is low, sales difficulty, what require quality of gasoline along with country improves constantly, and the sulphur content as the methyl tertiary butyl ether of gasoline dope must be reduced to and be less than 10ppm, therefore desulfurization process need be carried out to methyl tert-butyl ether product, to meet the need of market.
Patent CN201110082079 relates to a kind of method that catalytic distillation removes methyl tertiary butyl ether medium sulphide content.Adopt catalytic distillation thionizer reactor, methyl tertiary butyl ether with gas phase from charging at the bottom of tower, catalyzer is from tower top liquid phase feeding and methyl tertiary butyl ether counter current contact and by oxygenant effect, organic sulfide methyl tertiary butyl ether is oxidized to water soluble sulfate, water soluble sulfate is formed after oxidation, and be dissolved in the water after hydrogen peroxide reduction, stay at the bottom of tower, remove the methyl tertiary butyl ether of sulfide and a small amount of water in catalytic tower rectifying section rectifying separation, obtain the methyl tert-butyl ether product of high purity, low sulfur content from tower top.The catalyzer that the method uses is acidic substance, require higher to reactor material, oxygenant is the hydrogen peroxide of strong oxidizing property, meet methyl tertiary butyl ether easily to cause danger, use the method for the invention, the sulphur content of the methyl tert-butyl ether product produced is minimum can only reach 12ppm, and water content is higher.
The nitrate of metallic element Cu, Ag, Ni adopts pickling process to load on sorbent material by patent CN201310097098, and described sorbent material is silica gel, SBA series and MCM Series Molecules sieve.Then at 100 DEG C ~ 120 DEG C, drying is heated, the sorbent material obtained after drying load salpeter solution by a certain percentage under stirring at room temperature condition, sorbent material after load completes and methyl tertiary butyl ether react, can sulfide in deep removal methyl tertiary butyl ether.Sorbent material can recycle after adopting nitrogen heating stripping drying regeneration.The method of the invention is applicable to processing the lower methyl tertiary butyl ether of sulphur content, and sorbent material uses pickling process preparation, complicated process of preparation, cost is higher, preparation process use concentrated nitric acid, both dangerous also not environmentally, and be sorbent usedly applicable to batch technology, be not suitable for suitability for industrialized production.
Methyl tertiary butyl ether raw materials for production are the liquefied gas containing iso-butylene, it may be hydrogen sulfide that liquefied gas contains sulfide, carbonylsulfide, thiomethyl alcohol, sulfur alcohol, thioether, disulphide, the organic sulfides such as thiophene, MTBE total sulfur finally can be caused higher, each methyl tertiary butyl ether factory raw material sources are different, the sulfur speciation of its product is also different, the invention provides one and will not contain carbonylsulfide, containing thioether, disulphide, the organic sulfides such as thiophene, containing a small amount of mercaptan, the total sulfur content sulfide be greater than in the methyl tertiary butyl ether of 1000ppm is removed to the commercial run being less than 2ppm.
Summary of the invention
A kind of catalytic distillation is the object of the present invention is to provide to add the method for adsorbing and removing methyl tertiary butyl ether medium sulphide content, flow process of the present invention is simple, less investment, catalyzer, absorbent preparation are easy, sweetening effectiveness good, methyl tertiary butyl ether yield is greater than 99.8%, is applicable to industrialization continuous seepage.
The method that catalytic distillation of the present invention adds adsorbing and removing methyl tertiary butyl ether medium sulphide content is: first by catalytic distillation, the lightweight mercaptan in methyl tertiary butyl ether is converted into heavy sulphur under catalyst action, again heavy sulphur is separated with methyl tertiary butyl ether, isolated methyl tertiary butyl ether enters adsorption tower and adsorbs under sorbent material effect, thus removing lightweight sulphur, finally obtain low-sulfur methyl tertiary butyl ether.
Lightweight mercaptan: mainly refer to that boiling point is lower than the mercaptan of 55.3 DEG C.
Heavy sulphur: mainly refer to that boiling point is higher than the thioether, disulphide, thiophene etc. of 55.3 DEG C.
Lightweight sulphur: mainly refer to hydrogen sulfide, lightweight mercaptan etc.
Described catalyzer is that the mixing of sheet cocoanut active charcoal, four sulfonated phthalocyanine cobalts and NaOH solution is obtained, and each component content is in the catalyst: by weight percentage, four sulfonated phthalocyanine cobalts 0.5 ~ 3%; NaOH1 ~ 10%; Sheet cocoanut active charcoal is surplus.
Four sulfonated phthalocyanine cobalts are dissolved in NaOH solution by the preparation method of described catalyzer, after dipping sheet cocoanut active charcoal, then vacuum-drying, can finished catalyst be obtained.
Concrete steps are: be dissolved in NaOH solution by four sulfonated phthalocyanine cobalts, be poured into again in sheet cocoanut active charcoal and leave standstill 12 ~ 24h, then it is 60 ~ 90 DEG C in temperature, preferably 70 ~ 80 DEG C, relative vacuum degree is-0.095 ~-0.07MPa, preferably carry out vacuum drying treatment 8 ~ 12h under-0.09 ~-0.08MPa, can finished catalyst be obtained.
Described sorbent material comprises powdered active carbon and Fe
2o
3h
2o, when preparing sorbent material, by weight percentage, powdered active carbon 10 ~ 50%, preferably 25 ~ 35%; Fe
2o
3h
2o is surplus.
The preparation method of described sorbent material is at Fe
2o
3h
2active carbon powder and additive is added in O, then by making sorbent material after mixed grind, shaping, drying.
The preparation method of described sorbent material comprises the following steps:
1. adsorbent-shaping:
By Fe
2o
3h
2o and active carbon powder mix, then add additive wherein, and mediate evenly, extruded moulding, the catalyzer after shaping is cylindrical shape outward appearance;
2. dry:
Under sorbent material after shaping is placed in room temperature, naturally dry through 24 ~ 48h;
3. vacuum-drying:
Dried sorbent material is 60 ~ 90 DEG C in temperature, preferably 70 ~ 80 DEG C, and relative vacuum degree is-0.095 ~-0.07MPa, and preferred relative vacuum degree is carry out vacuum drying treatment under-0.09 ~-0.08MPa, can obtain finished product sorbent material.
The method that catalytic distillation of the present invention adds adsorbing and removing methyl tertiary butyl ether medium sulphide content comprises the following steps:
Catalyzer is put into catalytic distillation tower, sorbent material is put into adsorption tower, catalytic distillation tower epimere is methyl tertiary butyl ether rectifying section, middle part is conversion zone, fall at the bottom of tower be converted into the higher heavy sulphur of boiling point under the effect of conversion zone lightweight mercaptan at catalyzer after, tower top temperature is at 50 ~ 90 DEG C, preferably 60 ~ 70 DEG C, tower top pressure is 0 ~ 0.3MPa, preferably 0 ~ 0.1MPa, methyl tertiary butyl ether vapor-phase product refluxes through cooling rear portion at rectifying tower top, reflux ratio is 0.5 ~ 10, preferably 0.5 ~ 2, a part enters adsorption tower at the bottom of adsorption tower tower, adsorption tower atmospheric operation, temperature is 35 ~ 50 DEG C, preferably 40 ~ 45 DEG C, air speed is 1 ~ 5h
-1, preferably 1 ~ 3h
-1, adsorption tower overhead product is low-sulfur methyl tertiary butyl ether.
Beneficial effect of the present invention is as follows:
The present invention adopts catalytic distillation to add the combination process process of absorption, first in the reactor the lightweight mercaptan in methyl tertiary butyl ether is converted into heavy sulphur by the mode of catalytic distillation, heavy sulphur is separated with methyl tertiary butyl ether, and then enters absorption tower adsorbs and fall lightweight sulphur in methyl tertiary butyl ether.
The active ingredient of catalyzer of the present invention is four sulfonated phthalocyanine cobalts; Sorbent material is the two-element active component of the oxide compound containing powdered active carbon and iron, adopts kneading method preparation.The preparation technology of catalyzer and sorbent material is easy, safe preparation process environmental protection, and active ingredient is uniformly dispersed in the carrier, not easily runs off, and adds activity and the stability of catalyzer and sorbent material.
Compared with prior art, flow process of the present invention is simpler, and cost of investment is lower, is applicable to suitability for industrialized production; And the total sulfur in methyl tertiary butyl ether can be down to below 2ppm, reach the demand of mediation high-grade gasoline and follow-up deep processing and utilization.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention;
Wherein: 1, catalytic distillation tower; 2, adsorption tower; 3, beds; 4, adsorption tower feedstock transportation pump; 5, methyl tertiary butyl ether feedstock transportation pump; 6, methyl tertiary butyl ether raw material; 7, catalytic distillation tower liftout; 8, heavy sulphur; 9, low-sulfur methyl tert-butyl ether product.
Embodiment
Below in conjunction with embodiment, the present invention is described further.
Raw material in embodiment is that containing organic sulfides such as thioether, disulphide, thiophene, containing a small amount of mercaptan, total sulfur content is greater than the methyl tertiary butyl ether that 1000ppm is less than 3000ppm not containing carbonylsulfide.
Embodiment 1
The preparation of catalyzer: first preparing massfraction is the NaOH solution 50g of 5%, stir pours in the beaker filling four sulfonated phthalocyanine cobalts after NaOH dissolves completely, the weight of four sulfonated phthalocyanine cobalts is 1g, after stirring and dissolving, pour into after leaving standstill 24h in 96.5g sheet cocoanut active charcoal, then putting into vacuum drying oven, is-0.09MPa in vacuum tightness, temperature is under the condition of 80 DEG C dry 12 hours, obtained finished catalyst.
The preparation of sorbent material: by 10g powdered active carbon and 90gFe
2o
3h
2the sesbania dried bean noodles of O and 3.5g uses banded extruder extruded moulding, drying at room temperature 24h after mixing and mixing.Then putting into vacuum drying oven, is-0.09MPa in vacuum tightness, and temperature is dry 12h under the condition of 70 DEG C, and obtained finished product sorbent material, adsorption tower put into by sorbent material.
Catalytic distillation thionizer reactor diameter is 25mm, and height is 3000mm, and stage number is 45 pieces, and stainless steel θ ring filler is housed, and at the beds of the position of the 25th block of column plate filling 350mm, raw material methyl tertiary butyl ether is from beds underfeed.Beds epimere is methyl tertiary butyl ether rectifying section, tower top temperature is at 70 DEG C, tower top pressure is 0.1MPa, rectifying tower bottom product is high-sulfur product, and high-purity methyl tertiary butyl ether vapor-phase product refluxes through cooling rear portion at rectifying tower top, and reflux ratio is 2, a part enters adsorption tower at the bottom of adsorption tower tower, adsorption tower atmospheric operation, temperature is 40 DEG C, and air speed is 3h
-1, adsorption tower overhead product is high-purity low-sulphur methyl tert-butyl ether product.Total sulfur content by analysis in methyl tertiary butyl ether is reduced to 2ppm.
Embodiment 2
The preparation of catalyzer: first preparing massfraction is the NaOH solution 50g of 2%, stir pours in the beaker filling four sulfonated phthalocyanine cobalts after NaOH dissolves completely, the weight of four sulfonated phthalocyanine cobalts is 0.5g, after stirring and dissolving, pour into after leaving standstill 24h in 98.5g sheet cocoanut active charcoal, then putting into vacuum drying oven, is-0.085MPa in vacuum tightness, temperature is dry 12h under the condition of 80 DEG C, obtained finished catalyst.
Absorbent preparation: by 50g powdered active carbon and 50gFe
2o
3h
2the sesbania dried bean noodles of O and 3.0g uses banded extruder extruded moulding, drying at room temperature 36h after mixing and mixing.Then putting into vacuum drying oven, is-0.08MPa in vacuum tightness, and temperature is dry 12h under the condition of 70 DEG C, and obtained finished product sorbent material, adsorption tower put into by sorbent material.
Catalytic distillation thionizer reactor diameter is 25mm, and height is 3000mm, and stage number is 45 pieces, and stainless steel θ ring filler is housed, and at the beds of the position of the 25th block of column plate filling 350mm, raw material methyl tertiary butyl ether is from beds underfeed.Beds epimere is methyl tertiary butyl ether rectifying section, tower epimere is methyl tertiary butyl ether rectifying section, tower top temperature is at 60 DEG C, and tower top pressure is 0.05MPa, and rectifying tower bottom product is high-sulfur product, and high-purity methyl tertiary butyl ether vapor-phase product refluxes through cooling rear portion at rectifying tower top, reflux ratio is 3, and a part enters adsorption tower, adsorption tower atmospheric operation at the bottom of adsorption tower tower, temperature is 40 DEG C, and air speed is 2h
-1, adsorption tower overhead product is high-purity low-sulphur methyl tert-butyl ether product.Total sulfur content by analysis in methyl tertiary butyl ether does not detect.
Embodiment 3
The preparation of catalyzer: first preparing massfraction is the NaOH solution 50g of 10%, stir pours in the beaker filling four sulfonated phthalocyanine cobalts after NaOH dissolves completely, the weight of four sulfonated phthalocyanine cobalts is 3g, after stirring and dissolving, pour into after leaving standstill 24h in 92g sheet cocoanut active charcoal, then putting into vacuum drying oven, is-0.07MPa in vacuum tightness, temperature is dry 12h under the condition of 90 DEG C, obtained finished catalyst.
The preparation of sorbent material: by 25g powdered active carbon and 75gFe
2o
3h
2the sesbania dried bean noodles of O and 3.0g uses banded extruder extruded moulding, drying at room temperature 36h after mixing and mixing.Then putting into vacuum drying oven, is-0.07MPa in vacuum tightness, and temperature is dry 12h under the condition of 90 DEG C, and obtained finished product sorbent material, adsorption tower put into by sorbent material.
Catalytic distillation thionizer reactor diameter is 25mm, and height is 3000mm, and stage number is 45 pieces, and stainless steel θ ring filler is housed, and at the beds of the position of the 25th block of column plate filling 350mm, raw material methyl tertiary butyl ether is from beds underfeed.Beds epimere is methyl tertiary butyl ether rectifying section, tower top temperature is at 70 DEG C, tower top pressure is 0.2MPa, rectifying tower bottom product is high-sulfur product, and high-purity methyl tertiary butyl ether vapor-phase product refluxes through cooling rear portion at rectifying tower top, and reflux ratio is 1, a part enters adsorption tower at the bottom of adsorption tower tower, adsorption tower atmospheric operation, temperature is 40 DEG C, and air speed is 2h
-1, adsorption tower overhead product is high-purity low-sulphur methyl tert-butyl ether product.Total sulfur content by analysis in methyl tertiary butyl ether is reduced to 2ppm.
Embodiment 4
The preparation of catalyzer: first preparing massfraction is the NaOH solution 50g of 20%, stir pours in the beaker filling four sulfonated phthalocyanine cobalts after NaOH dissolves completely, the weight of four sulfonated phthalocyanine cobalts is 2g, after stirring and dissolving, pour into after leaving standstill 24h in 88g sheet cocoanut active charcoal, then putting into vacuum drying oven, is-0.08MPa in vacuum tightness, temperature is dry 12h under the condition of 90 DEG C, obtained finished catalyst.
The preparation of sorbent material: by 35g powdered active carbon and 65gFe
2o
3h
2the sesbania dried bean noodles of O and 4.0g uses banded extruder extruded moulding, drying at room temperature 40h after mixing and mixing.Then putting into vacuum drying oven, is-0.09MPa in vacuum tightness, and temperature is dry 12h under the condition of 80 DEG C, and obtained finished product sorbent material, adsorption tower put into by sorbent material.
Catalytic distillation thionizer reactor diameter is 25mm, and height is 3000mm, and stage number is 45 pieces, and stainless steel θ ring filler is housed, and at the beds of the position of the 25th block of column plate filling 350mm, raw material methyl tertiary butyl ether is from beds underfeed.Beds epimere is methyl tertiary butyl ether rectifying section, tower top temperature is at 65 DEG C, tower top pressure is pressure-fired, rectifying tower bottom product is high-sulfur product, and high-purity methyl tertiary butyl ether vapor-phase product refluxes through cooling rear portion at rectifying tower top, and reflux ratio is 3, a part enters adsorption tower at the bottom of adsorption tower tower, adsorption tower atmospheric operation, temperature is 40 DEG C, and air speed is 1h
-1, adsorption tower overhead product is high-purity low-sulphur methyl tert-butyl ether product.Total sulfur content by analysis in methyl tertiary butyl ether is not for detect.
Claims (8)
1. a catalytic distillation adds the method for adsorbing and removing methyl tertiary butyl ether medium sulphide content, it is characterized in that: the lightweight mercaptan in methyl tertiary butyl ether is first converted into heavy sulphur by catalytic distillation by the method under catalyst action, again heavy sulphur is separated with methyl tertiary butyl ether, isolated methyl tertiary butyl ether enters adsorption tower and adsorbs under sorbent material effect, thus removing lightweight sulphur, finally obtain low-sulfur methyl tertiary butyl ether.
2. catalytic distillation according to claim 1 adds the method for adsorbing and removing methyl tertiary butyl ether medium sulphide content, it is characterized in that: described catalyzer is that the mixing of sheet cocoanut active charcoal, four sulfonated phthalocyanine cobalts and NaOH solution is obtained, each component content is in the catalyst: by weight percentage, four sulfonated phthalocyanine cobalts 0.5 ~ 3%; NaOH1 ~ 10%; Sheet cocoanut active charcoal is surplus.
3. catalytic distillation according to claim 2 adds the method for adsorbing and removing methyl tertiary butyl ether medium sulphide content, it is characterized in that: four sulfonated phthalocyanine cobalts are dissolved in NaOH solution by the preparation method of described catalyzer, after dipping sheet cocoanut active charcoal, vacuum-drying again, can obtain finished catalyst.
4. catalytic distillation according to claim 3 adds the method for adsorbing and removing methyl tertiary butyl ether medium sulphide content, it is characterized in that: four sulfonated phthalocyanine cobalts are dissolved in NaOH solution by the preparation method of described catalyzer, be poured into again in sheet cocoanut active charcoal and leave standstill 12 ~ 24h, then it is 60 ~ 90 DEG C in temperature, relative vacuum degree is carry out vacuum drying treatment 8 ~ 12h under-0.095 ~-0.07MPa, can obtain finished catalyst.
5. catalytic distillation according to claim 1 adds the method for adsorbing and removing methyl tertiary butyl ether medium sulphide content, it is characterized in that: described sorbent material comprises powdered active carbon and Fe
2o
3h
2o, when preparing sorbent material, by weight percentage, powdered active carbon is 10 ~ 50%, Fe
2o
3h
2o is surplus.
6. catalytic distillation according to claim 5 adds the method for adsorbing and removing methyl tertiary butyl ether medium sulphide content, it is characterized in that: the preparation method of described sorbent material is at Fe
2o
3h
2active carbon powder and additive is added in O, then by making sorbent material after mixed grind, shaping, drying.
7. catalytic distillation according to claim 6 adds the method for adsorbing and removing methyl tertiary butyl ether medium sulphide content, it is characterized in that: the preparation method of described sorbent material comprises the following steps:
1. adsorbent-shaping:
By Fe
2o
3h
2o and active carbon powder mix, then add additive wherein, and mediate evenly, extruded moulding, the catalyzer after shaping is cylindrical shape outward appearance;
2. dry:
Under sorbent material after shaping is placed in room temperature, naturally dry through 24 ~ 48h;
3. vacuum-drying:
Dried sorbent material is 60 ~ 90 DEG C in temperature, and relative vacuum degree is carry out vacuum drying treatment under-0.095 ~-0.07MPa, can obtain finished product sorbent material.
8. add the method for adsorbing and removing methyl tertiary butyl ether medium sulphide content according to the arbitrary described catalytic distillation of claim 1-7, it is characterized in that: the method comprises the following steps:
Catalyzer is put into catalytic distillation tower, sorbent material is put into adsorption tower; Catalytic distillation tower epimere is methyl tertiary butyl ether rectifying section, middle part is conversion zone, fall at the bottom of tower be converted into heavy sulphur under the effect of conversion zone lightweight mercaptan at catalyzer after, tower top temperature is at 50 ~ 90 DEG C, and tower top pressure is 0 ~ 0.3MPa, methyl tertiary butyl ether vapor-phase product refluxes through cooling rear portion at rectifying tower top, reflux ratio is 0.5 ~ 10, and a part enters adsorption tower, adsorption tower atmospheric operation at the bottom of adsorption tower tower, temperature is 35 ~ 50 DEG C, and air speed is 1 ~ 5h
-1, adsorption tower overhead product is low-sulfur methyl tertiary butyl ether.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410248147.2A CN105272832A (en) | 2014-06-06 | 2014-06-06 | Method for removing sulfides in methyl tert-butyl ether through catalytic distillation and adsorption |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410248147.2A CN105272832A (en) | 2014-06-06 | 2014-06-06 | Method for removing sulfides in methyl tert-butyl ether through catalytic distillation and adsorption |
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|---|---|
| CN105272832A true CN105272832A (en) | 2016-01-27 |
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|---|---|---|---|
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1986059A (en) * | 2005-12-23 | 2007-06-27 | 中国石油化工股份有限公司 | Preparing process of mercaptol oxidizing catalyst |
| CN101705108A (en) * | 2009-12-11 | 2010-05-12 | 郝天臻 | Liquid hydrocarbon mercaptan removal technique capable of deeply removing total sulfur |
| CN102491882A (en) * | 2011-12-02 | 2012-06-13 | 河北精致科技有限公司 | Method for producing low-sulfur methyl tertiary butyl ether |
| CN102731268A (en) * | 2011-04-01 | 2012-10-17 | 北京石油化工学院 | Method for removing sulfide in methyl tert butyl ether by catalytic distillation |
| CN103524310A (en) * | 2013-10-16 | 2014-01-22 | 凯瑞化工股份有限公司 | Deep desulfurization method of MTBE (Methyl Tert-Butyl Ether) |
-
2014
- 2014-06-06 CN CN201410248147.2A patent/CN105272832A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1986059A (en) * | 2005-12-23 | 2007-06-27 | 中国石油化工股份有限公司 | Preparing process of mercaptol oxidizing catalyst |
| CN101705108A (en) * | 2009-12-11 | 2010-05-12 | 郝天臻 | Liquid hydrocarbon mercaptan removal technique capable of deeply removing total sulfur |
| CN102731268A (en) * | 2011-04-01 | 2012-10-17 | 北京石油化工学院 | Method for removing sulfide in methyl tert butyl ether by catalytic distillation |
| CN102491882A (en) * | 2011-12-02 | 2012-06-13 | 河北精致科技有限公司 | Method for producing low-sulfur methyl tertiary butyl ether |
| CN103524310A (en) * | 2013-10-16 | 2014-01-22 | 凯瑞化工股份有限公司 | Deep desulfurization method of MTBE (Methyl Tert-Butyl Ether) |
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Application publication date: 20160127 |