CN204454944U - A kind of desulfurizer of sulfur methyl tertiary butyl ether product - Google Patents
A kind of desulfurizer of sulfur methyl tertiary butyl ether product Download PDFInfo
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Abstract
The utility model discloses a kind of desulfurizer of sulfur methyl tertiary butyl ether product, comprise sulfur-bearing MTBE feed-pipe, distillation tower A, condenser, return tank, distillation tower B, reboiler A and reboiler B; Described sulfur-bearing MTBE feed-pipe is connected to the middle and lower part of distillation tower A, and distillation tower A tower top outlet is connected to condenser inlet, and condensator outlet is connected to return tank entrance, and return tank outlet is connected to trim the top of column pipe and low-sulfur MTBE finished product output tube respectively; Bottom described distillation tower A, liquid outlet connects reboiler A and second distillation carrier pipe respectively, and the other end of second distillation carrier pipe is connected to distillation tower B top; Described distillation tower B tower top outlet is connected to the bottom of distillation tower A, and the bottom liquid outlet of distillation tower B connects reboiler B and hydrogenation pipe respectively; This device adopts double-column process, and the column bottom temperature of first tower is low, adopts low temperature exhaust heat heating, thus has saved heating steam consumption, decrease tooling cost.
Description
Technical field
The utility model relates to a kind of methyl tertbutyl ether production equipment, specifically a kind of desulfurizer of sulfur methyl tertiary butyl ether product.
Background technology
MTBE is commonly called as methyl tertiary butyl ether, is a kind of colourless, transparent, high-octane liquid.Main be used as to produce unleaded, stop bracket gasoline ideal blending component and cracking for the industrial chemicals of high-purity iso-butylene.Molecular formula CH3OC (CH3) 3, relative molecular weight 88.15, fusing point-109 DEG C, boiling point 55.2 DEG C, CAS NO.:1634-04-4.MTBE oxygen level 18.2%, during blending high-grade gasoline, add-on is generally between 10-20%.
The MTBE product sulphur content being made raw material production by oil refining carbon four is generally higher, 100 low ~ 200ppm, 2000 high ~ 3000ppm.Can not meet state's V content of sulfur in gasoline be less than 10ppm index requirement (state V content of sulfur in gasoline require be less than 10ppm, MTBE sulphur content as state V gasoline concoction component also needs to be less than the production blending that 10ppm just can not affect high grade low-sulphur oil), so, MTBE desulfurization uses with satisfied blending state V gasoline, is the inevitable choice of MTBE production from now on.
MTBE is synthesized under cation exchange resin catalyst effect by the iso-butylene in carbon four raw material and methyl alcohol, so the sulphur content in MTBE derives from methyl alcohol, mixed c 4 and resin catalyst respectively.
Methyl alcohol sulphur content at present for the synthesis of MTBE is generally less than 5ppm.The sulphur content of indivedual enterprises methyl alcohol also up to 50ppm, and can contain more hydrogen sulfide and carbonylsulfide sometimes.Hydrogen sulfide and carbonylsulfide can form isobutyl mercaptan with iso-butylene under MTBE synthetic reaction condition, and this is also the main source of isobutyl mercaptan content in MTBE.But, the sulphur content of methyl alcohol is less than 5ppm under normal circumstances, is less than 2 ppm to the contribution of MTBE sulphur content, so it is not the principal element that MTBE sulphur content is high.
Cation exchange resin catalyst is made up of two essential parts, can represent with skeleton symbol R-SO3H, and R is the polymeric matrix with cross-linked structure, and SO3H is the sulfonic acid group with katalysis, and sulfonic acid group can come off being more than or equal to 80 DEG C.The sulfonic group come off can cause sulphur increase about 7.7mg/kg in MTBE product.The speed that under normal operating condition, sulfonic acid group comes off, far below this value, generally more than 5mg/kg, can not neither cause the principal element that MTBE sulphur content is high by the sulfonic acid group sulphur content increase caused that comes off.
The MTBE sulphur content of being produced by chemical industry carbon four is at present general all very low, substantially all within 10ppm.And the MTBE sulphur content of producing with refinery C four is generally low at 100 ~ 200ppm, high reaches 2000 ~ 3000ppm.Visible, the sulphur in MTBE is mainly derived from mixed c 4.
Be mainly derived from the deduction of carbon four according to MTBE sulfide, in MTBE, should thiomethyl alcohol, sulfur alcohol, dimethyl sulfide and disulphide be contained.Actual analysis finds except disulphide, and thiomethyl alcohol, sulfur alcohol, dimethyl sulfide seldom occur; This is because first, sulfur alcohol is comparatively active, in MTBE synthetic environment easily and isobutene reaction form the very high methyl-tert butyl sulfide of boiling point and the tertiary butyl sulfide of ethyl; Do not react these three kinds of sulfide of conversion, because boiling point is lower, after MTBE and ether in carbon four fractionation by distillation process, compare tendency yet and to be separated to after ether in carbon four.In addition the sulfide of carbonylsulfide, isobutyl mercaptan and other not clear forms is also found that there is in MTBE.Carbonylsulfide and these two kinds of sulfide of isobutyl mercaptan are mainly derived from methanol feedstock, and isobutyl mercaptan is mainly formed with butylene under MTBE synthetic reaction condition by the hydrogen sulfide in methyl alcohol and carbonylsulfide.What come off containing catalyzer in the sulfide of not clear form contains sulfonic product.
In order to meet the requirement of state V gasoline quality standard and chemical industry MTBE sulphur content, in recent years, it is very fast that sulphur technical development falls in domestic MTBE desulfurization, within 2011, State Intellectual Property Office discloses exquisite Science and Technology Ltd.'s " a kind of production method of the low sulfur methyl tertiary butyl ether " patented technology in Hebei, application number: 2011103976110, this technology adopts single tower extractive distillation desulfurization technology, this technology is adopted and the device gone into operation has 22 covers from extending to 10 ends in 2014, all reach the requirement of state five content of sulfur in gasoline lower than 10ppm, part is lower than 5ppm, obtain PetroChina Company Limited., the consistent favorable comment of the oil refining unit such as China Petrochemical Industry.But this technology has the following disadvantages simultaneously: the first, when distilling tower top reflux ratio and being less, partial devices can not reach chemical industry MTBE sulphur content and be less than 5ppm product requirement.The second, because distillation heating all adopts steam heating, so energy consumption cost is higher.
In July, 2013, State Intellectual Property Office disclosed PetroChina Company Ltd.'s " a kind of device removing higher boiling sulfur compound in methyl tertiary butyl ether " application number: 201220711913 utility model patent technology, although this technology adopts double tower distil desulfurization process.But this technology distillation tower 2 is independently distillation towers, because at the bottom of its charging and tower, sulphur content is higher, in order to reduce this overhead product sulphur content, by increasing the means of reflux ratio or increase tower height, thus energy consumption and infrastructure investment can only be too increased, the also reduction of unfavorable high-sulfur byproduct yield.
Utility model content
The purpose of this utility model is the desulfurizer providing a kind of sulfur methyl tertiary butyl ether product, to solve the problem proposed in above-mentioned background technology.
For achieving the above object, the utility model provides following technical scheme:
A desulfurizer for sulfur methyl tertiary butyl ether product, comprises sulfur-bearing MTBE feed-pipe, distillation tower A, condenser, return tank, distillation tower B, reboiler A and reboiler B; Described sulfur-bearing MTBE feed-pipe is connected to the middle and lower part of distillation tower A, distillation tower A tower top outlet is connected to condenser inlet, condensator outlet is connected to return tank entrance, return tank outlet is connected to trim the top of column pipe and low-sulfur MTBE finished product output tube respectively, and the other end of trim the top of column pipe is connected to the upper end refluxing opening of distillation tower A; Bottom described distillation tower A, liquid outlet connects reboiler A and second distillation carrier pipe respectively, and the outlet of reboiler A is connected to distillation tower A lower end, and the other end of second distillation carrier pipe is connected to distillation tower B top; Described distillation tower B tower top outlet is connected to the bottom of distillation tower A by second distillation discharge nozzle, the bottom liquid outlet of distillation tower B connects reboiler B and hydrogenation pipe respectively, the outlet of reboiler B is connected to the lower end of distillation tower B, and the other end of hydrogenation pipe is connected to hydrogenating materials tank.
As further program of the utility model: described distillation tower A uses low temperature exhaust heat as thermal source.
As the utility model further scheme: the desulfurizer of described sulfur methyl tertiary butyl ether product also comprises extraction antigum inhibitor tank (2), described extraction antigum inhibitor tank connects sulfur-bearing MTBE feed-pipe by pipeline.
Compared with prior art, the beneficial effects of the utility model are: 1, the desulfurizer of described sulfur methyl tertiary butyl ether product adopts double-column process, the column bottom temperature of first tower, lower than 80 DEG C, can heat with low temperature exhaust heat at the bottom of tower, thus greatly save heating steam consumption.80% of the required heating load of distillation is provided by low temperature exhaust heat, and all the other loads of 20% are provided by steam, thus save the steam consumption of more than 80%, decrease tooling cost; 2, the height of stripping section determines the height of byproduct yield, the desulfurizer of described sulfur methyl tertiary butyl ether product utilizes the advantage of double tower, stripping section is increased further, thus reduce further the productive rate of byproduct, guaranteeing that sulphur content in MTBE product drops to the specification of quality of below 5ppm, yield can reach more than 99.8%, reduce further tooling cost.
Accompanying drawing explanation
Fig. 1 is the structural representation of the desulfurizer of sulfur methyl tertiary butyl ether product.
In figure: 1-sulfur-bearing MTBE feed-pipe, 2-extract antigum inhibitor tank, 3-distillation tower A, 4-condenser, 5-return tank, 6-trim the top of column pipe, 7-low-sulfur MTBE finished product output tube, 8-second distillation discharge nozzle, 9-distillation tower B, 10-hydrogenation pipe, 11-reboiler B, 12-second distillation carrier pipe, 13-reboiler A.
Embodiment
Below in conjunction with the accompanying drawing in the utility model embodiment, be clearly and completely described the technical scheme in the utility model embodiment, obviously, described embodiment is only the utility model part embodiment, instead of whole embodiments.Based on the embodiment in the utility model, those of ordinary skill in the art are not making the every other embodiment obtained under creative work prerequisite, all belong to the scope of the utility model protection.
Refer to Fig. 1, in the utility model embodiment, a desulfurizer for sulfur methyl tertiary butyl ether product, comprises sulfur-bearing MTBE feed-pipe 1, extraction antigum inhibitor tank 2, distillation tower A 3, condenser 4, return tank 5, distillation tower B 9, reboiler A 13 and reboiler B 11, described sulfur-bearing MTBE feed-pipe 1 is connected to the middle and lower part of distillation tower A 3, extraction antigum inhibitor tank 2 connects sulfur-bearing MTBE feed-pipe 1 by pipeline, sulfur-bearing MTBE product flows in distillation tower A3 through sulfur-bearing MTBE feed-pipe 1, extraction antigum inhibitor in extraction antigum inhibitor tank 2 is mixed together with sulfur-bearing MTBE product and enters distillation tower A 3 and carry out single flash after volume pump boosting, distillation tower A 3 tower top outlet is connected to condenser 4 entrance, condenser 4 outlet is connected to return tank 5 entrance, return tank 5 exports and is connected to trim the top of column pipe 6 and low-sulfur MTBE finished product output tube 7 respectively, the other end of trim the top of column pipe 6 is connected to the upper end refluxing opening of distillation tower A 3, sulfur-bearing MTBE product carries out single flash in distillation tower A 3, single flash ensures that the MTBE of charging about 80% is vaporized, the low-sulfur MTBE of distillation tower A 3 tower top is after condenser 4 is condensed to about 55 DEG C, enter return tank of top of the tower 5, control return tank 5 pressure at about 0.02Mpa, liquid phase low-sulfur MTBE is after reflux pump boosting, a part is as distillation tower A 3 trim the top of column, distillation tower A 3 is back to through trim the top of column pipe 6, a part sends into low-sulfur MTBE finished product output tube 7 as product, low-sulfur MTBE products pot is delivered to after water cooler is cooled to about 40 DEG C,
Bottom described distillation tower A 3, liquid outlet connects reboiler A 13 and second distillation carrier pipe 12 respectively, the outlet of reboiler A 13 is connected to distillation tower A 3 lower end, the other end of second distillation carrier pipe 12 is connected to distillation tower B 9 top, why be connected to the top of distillation tower B 9, to improve stripping section, the remaining about 20% sulfur-bearing MTBE product of not vaporizing in bottom distillation tower A 3, extraction antigum inhibitor and sulfide are delivered to distillation tower B 9 by second distillation carrier pipe 12 and are carried out second distillation, the column bottom temperature of distillation tower A 3 is about 75 DEG C, because the column bottom temperature of distillation tower A 3 is below 80 DEG C, distillation tower A 3 uses low temperature exhaust heat as thermal source, utilize the low-temperature heat source that the Ye Shi oil refining enterprise between 80 DEG C ~ 120 DEG C extensively has, greatly save the consumption of heating steam, in addition, because distillation tower A 3 bottom temp is lower, add that sulphur content is also lower, so from distillation tower A 3 top, the more single tower process of product sulphur content is out lower, general at below 5ppm,
Described distillation tower B 9 tower top outlet is connected to the bottom of distillation tower A 3 by second distillation discharge nozzle 8, the bottom liquid outlet of distillation tower B 9 connects reboiler B 11 and hydrogenation pipe 10 respectively, the outlet of reboiler B 11 is connected to the lower end of distillation tower B 9, the other end of hydrogenation pipe 10 is connected to hydrogenating materials tank, in distillation tower B 9, the components such as extraction antigum inhibitor and the MTBE that do not vaporize are by sulfate layer flows downhill, MTBE vaporizes gradually, at the bottom of tower, MTBE substantially all vaporizes, be enriched sulfide, byproduct at the bottom of distillation tower B 9 tower of extraction antigum inhibitor and other heavy constituents, enter bottom reboiler B 11 to reheat, make MTBE all vaporize as far as possible, and part heavy constituent is vaporized, for distillation provides vapour phase load, MTBE after gasification rises to distillation tower B 9 top, and deliver to distillation tower A 3 bottom by second distillation discharge nozzle 8, at the bottom of tower, remaining byproduct delivers to hydrogenating materials tank through hydrogenation pipe 10.The low sulfur-bearing vapour phase that distillation tower B 9 top obtains turns back to the bottom of distillation tower A 3, and such distillation tower B 9 does not need to establish top backflow and auxiliary facility, does not need too many separation progression simultaneously yet.By adjustment column bottom temperature, in liquid phase at the bottom of control tower, the content of MTBE is below 5%.Column bottom temperature is relevant to by-product yields, and by-product yields is less, and column bottom temperature is higher, and general control is within 120 DEG C, and under the prerequisite meeting overhead product sulphur content index, the amount of by product is more low better, and by product can be discharged continuously, also can be interrupted discharge.The heavy constituent that the byproduct of distillation desulfurization is mainly contained in MTBE, as TBA2 ~ 5%, DIB50 ~ 60%, sulfide 10 ~ 20%, extraction antigum inhibitor 10 ~ 20%, wherein the total amount of MTBE and MSBE is generally below 10%.
Described distillation tower B 9 adopts low-pressure steam as thermal source.Because distillation tower B 9 inlet amount is only about 20% of feedstock amount, so distill for desulfurizer for a whole set of MTBE, steam consumption is significantly reduced.
Principle of work of the present utility model is: the desulfurizer of described sulfur methyl tertiary butyl ether product, sulfur-bearing MTBE product flows in distillation tower A 3 through sulfur-bearing MTBE feed-pipe 1, extraction antigum inhibitor in extraction antigum inhibitor tank 2 is mixed together with sulfur-bearing MTBE product and enters distillation tower A 3 and carry out single flash after volume pump boosting, single flash ensures that the MTBE of charging about 80% is vaporized, the low-sulfur MTBE of distillation tower A 3 tower top is after condenser 4 is condensed to about 55 DEG C, enter return tank of top of the tower 5, control return tank 5 pressure at about 0.02Mpa, liquid phase low-sulfur MTBE is after reflux pump boosting, a part is as distillation tower A 3 trim the top of column, distillation tower A 3 is back to through trim the top of column pipe 6, a part sends into low-sulfur MTBE finished product output tube 7 as product, low-sulfur MTBE products pot is delivered to after water cooler is cooled to about 40 DEG C, the remaining about 20% sulfur-bearing MTBE product of not vaporizing in bottom distillation tower A 3, extraction antigum inhibitor and sulfide, deliver to distillation tower B 9 by second distillation carrier pipe 12 and carry out second distillation, in distillation tower B 9, extraction antigum inhibitor and the MTBE do not vaporized are by sulfate layer flows downhill, MTBE vaporizes gradually, at the bottom of tower, MTBE substantially all vaporizes, be enriched sulfide, byproduct at the bottom of distillation tower B 9 tower of extraction antigum inhibitor and other heavy constituents, enter bottom reboiler B 11 to reheat, make MTBE all vaporize as far as possible, and part heavy constituent is vaporized, for distillation provides vapour phase load, MTBE after gasification rises to distillation tower B 9 top, and deliver in distillation tower A 3 by second distillation discharge nozzle 8, at the bottom of tower, remaining byproduct delivers to hydrogenating materials tank through hydrogenation pipe 10.
The desulfurizer of described sulfur methyl tertiary butyl ether product adopts double-column process, and the column bottom temperature of first tower, lower than 80 DEG C, can heat with low temperature exhaust heat at the bottom of tower, thus greatly save heating steam consumption.Compare with single tower, MTBE steam consumption per ton is reduced to 40kg by 240kg, and energy consumption is marked oil/ton by 18kg and is reduced to below 10kg mark oil/ton.Only reduce steam consumption one, unit tooling cost MTBE per ton can save more than 30 yuan.
The height of stripping section determines the height of byproduct yield, the desulfurizer of described sulfur methyl tertiary butyl ether product utilizes the advantage of double tower, stripping section is increased further, thus reduce further the productive rate of byproduct, guaranteeing that sulphur content in MTBE product drops to the specification of quality of below 5ppm, yield can reach more than 99.8%.Only reduce by-product volume one, unit tooling cost can save 20 yuan/ton of MTBE.
Certain enterprise sulfur-bearing MTBE sulphur content 40 ~ 60ppm, sulfur-bearing MTBE is from synthesis unit, enter the desulfurizer of this sulfur methyl tertiary butyl ether product through synthesis unit base product Liquid level, extraction antigum inhibitor is mixed together with charging and carries out single flash into distillation tower A 3 after volume pump boosting.
Control distillation tower A 3 tower top pressure 0.05Mpa, distillation tower A 3 tower top low-sulfur MTBE enters return tank of top of the tower 5 after condenser 4 condenses to 54 DEG C.Liquid phase low-sulfur MTBE is after reflux pump boosting, and a part is as the backflow of distillation tower top, and a part, as the product feeding low-sulfur MTBE finished product output tube 7 after refining, after water cooler is cooled to 40 DEG C, delivers to low-sulfur MTBE finished pot.At the bottom of distillation tower A 3 tower, liquid phase major part adds thermogenesis vapour phase load through reboiler A 13, and wherein small part sends into second distillation carrier pipe 12, enters distillation tower B 9 carry out second distillation through intermediate feed pump and Liquid level.Concrete operations condition is as table 1.
Table 1: certain enterprise uses double-column process to contrast with using the parameters of single tower flow process
| Project name | Unit | Distillation tower A | Distillation tower B | Single tower |
| Pressure tower top | KPa | 150 | -- | 150.00 |
| Tower top temperature | ℃ | 67.4 | 74.5 | 69.1 |
| Cocurrent flow temperature | ℃ | 54.0 | -- | 54.0 |
| Column bottom temperature | ℃ | 74.4 | 119.9 | 102.2 |
| Feeding temperature | ℃ | 70.0 | 74.4 | 70.0 |
| Input rate | ％ | 100 | 15～30 | 100 |
| Cocurrent flow ratio | ％ | 0.2 | 0 | 0.5 |
| Overhead oil rate | ％ | 99.5 | 15～30 | 99.0 |
| Oil rate at the bottom of tower | ％ | 15～30 | 0.5 | 1.0 |
The material major part entering distillation tower B turns back at the bottom of distillation tower A tower in vapour phase mode, and small part high-sulfur component is after high-sulfur component water cooler cooling at the bottom of tower, and mountain high-sulfur component pump is extracted out and delivered to hydrogenation unit head tank.
MTBE sulphur content after this enterprise's desulfurization reaches 2 μ g/g, and mass yield is 99.92%.
To those skilled in the art, obvious the utility model is not limited to the details of above-mentioned one exemplary embodiment, and when not deviating from spirit of the present utility model or essential characteristic, can realize the utility model in other specific forms.Therefore, no matter from which point, all should embodiment be regarded as exemplary, and be nonrestrictive, scope of the present utility model is limited by claims instead of above-mentioned explanation, and all changes be therefore intended in the implication of the equivalency by dropping on claim and scope are included in the utility model.Any Reference numeral in claim should be considered as the claim involved by limiting.
In addition, be to be understood that, although this specification sheets is described according to embodiment, but not each embodiment only comprises an independently technical scheme, this narrating mode of specification sheets is only for clarity sake, those skilled in the art should by specification sheets integrally, and the technical scheme in each embodiment also through appropriately combined, can form other embodiments that it will be appreciated by those skilled in the art that.
Claims (3)
1. the desulfurizer of a sulfur methyl tertiary butyl ether product, comprise sulfur-bearing MTBE feed-pipe (1), distillation tower A (3), condenser (4), return tank (5), distillation tower B (9), reboiler A (13) and reboiler B (11), it is characterized in that: described sulfur-bearing MTBE feed-pipe (1) is connected to the middle and lower part of distillation tower A (3), distillation tower A (3) tower top outlet is connected to condenser (4) entrance, condenser (4) outlet is connected to return tank (5) entrance, return tank (5) outlet is connected to trim the top of column pipe (6) and low-sulfur MTBE finished product output tube (7) respectively, the other end of trim the top of column pipe (6) is connected to the upper end refluxing opening of distillation tower A (3), described distillation tower A (3) bottom liquid outlet connects reboiler A (13) and second distillation carrier pipe (12) respectively, the outlet of reboiler A (13) is connected to distillation tower A (3) lower end, and the other end of second distillation carrier pipe (12) is connected to distillation tower B (9) top, described distillation tower B (9) tower top outlet is connected to the bottom of distillation tower A (3) by second distillation discharge nozzle (8), the bottom liquid outlet of distillation tower B (9) connects reboiler B (11) and hydrogenation pipe (10) respectively, the outlet of reboiler B (11) is connected to the lower end of distillation tower B (9), and the other end of hydrogenation pipe (10) is connected to hydrogenating materials tank.
2. the desulfurizer of sulfur methyl tertiary butyl ether product according to claim 1, is characterized in that: described distillation tower A (3) uses low temperature exhaust heat as thermal source.
3. the desulfurizer of sulfur methyl tertiary butyl ether product according to claim 1, it is characterized in that: the desulfurizer of described sulfur methyl tertiary butyl ether product also comprises extraction antigum inhibitor tank (2), and described extraction antigum inhibitor tank (2) connects sulfur-bearing MTBE feed-pipe (1) by pipeline.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105777500A (en) * | 2016-05-25 | 2016-07-20 | 郝天臻 | Extraction anti-gum agent for MTBE desulfurization |
| CN107473938A (en) * | 2017-09-19 | 2017-12-15 | 中建安装工程有限公司 | Utilize the device and method of sulfide in dividing plate extractive distillation column methanol removal |
| CN108465259A (en) * | 2017-02-23 | 2018-08-31 | 山东京博石油化工有限公司 | A kind of methyl tertiary butyl ether(MTBE) desulphurization system and sulfur method |
| CN113786638A (en) * | 2021-10-18 | 2021-12-14 | 浙江美福石油化工有限责任公司 | MTBE product desulphurization unit |
| CN114712870A (en) * | 2022-03-17 | 2022-07-08 | 山东神驰石化有限公司 | MTBE desulfurization purification device |
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2014
- 2014-12-31 CN CN201420873941.1U patent/CN204454944U/en active Active
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105777500A (en) * | 2016-05-25 | 2016-07-20 | 郝天臻 | Extraction anti-gum agent for MTBE desulfurization |
| CN105777500B (en) * | 2016-05-25 | 2018-03-06 | 郝天臻 | A kind of extraction antigum inhibitor for MTBE desulfurization |
| CN108465259A (en) * | 2017-02-23 | 2018-08-31 | 山东京博石油化工有限公司 | A kind of methyl tertiary butyl ether(MTBE) desulphurization system and sulfur method |
| CN107473938A (en) * | 2017-09-19 | 2017-12-15 | 中建安装工程有限公司 | Utilize the device and method of sulfide in dividing plate extractive distillation column methanol removal |
| CN107473938B (en) * | 2017-09-19 | 2023-10-10 | 中建安装集团有限公司 | Device and method for removing sulfides in methanol by using partition plate extraction rectifying tower |
| CN113786638A (en) * | 2021-10-18 | 2021-12-14 | 浙江美福石油化工有限责任公司 | MTBE product desulphurization unit |
| CN114712870A (en) * | 2022-03-17 | 2022-07-08 | 山东神驰石化有限公司 | MTBE desulfurization purification device |
| CN114712870B (en) * | 2022-03-17 | 2024-02-20 | 山东神驰石化有限公司 | MTBE desulfurization purification device |
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