CN108218677B - Method and device for desulfurizing methyl tert-butyl ether - Google Patents

Method and device for desulfurizing methyl tert-butyl ether Download PDF

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CN108218677B
CN108218677B CN201611200858.8A CN201611200858A CN108218677B CN 108218677 B CN108218677 B CN 108218677B CN 201611200858 A CN201611200858 A CN 201611200858A CN 108218677 B CN108218677 B CN 108218677B
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rectification tower
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CN108218677A (en
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伊东
张玉东
王家杰
苗勇
田存轩
张尕玲
王吴斌
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Petrochina Co Ltd
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    • 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
    • C07C41/40—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation
    • C07C41/42—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation by distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation

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  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a method and a device for desulfurizing methyl tert-butyl ether. The method adopts a double-tower rectification process, wherein the double towers comprise a rectification tower A and a rectification tower B, the rectification tower A is a desulfurization tower, and the rectification tower B is an oxygen-containing compound recovery tower. The device comprises a rectification tower A and a rectification tower B which are sequentially communicated, wherein the rectification tower A is a desulfurization tower, and the rectification tower B is an oxygen-containing compound recovery tower. By applying the technical scheme of the invention, the double towers comprise a rectification tower A and a rectification tower B, the rectification tower A is a desulfurization tower, the rectification tower B is an oxygen-containing compound recovery tower, and the rectification tower B recovers the oxygen-containing compound which is a high-quality gasoline component and has considerable recovery value. Meanwhile, the technical problem that the tail material is treated by adopting a gasoline hydrogenation mode, and the service life of a hydrogenation catalyst is influenced because water is generated in the hydrogenation process of the oxygen-containing compound is solved.

Description

Method and device for desulfurizing methyl tert-butyl ether
Technical Field
The invention relates to the field of petrochemical industry, in particular to a method and a device for desulfurizing methyl tert-butyl ether.
Background
After the national V gasoline standard is comprehensively realized in 2017, gasoline with over-standard sulfur content cannot enter the market, so that low vulcanization of the gasoline becomes a trend. On the other hand, most refineries choose to blend MTBE (methyl-butyl ether) into gasoline in an amount of about 11% to 13% in order to meet the requirement of high octane number of gasoline, so sulfur in MTBE is also a non-negligible factor. The high-sulfur MTBE is desulfurized into low-sulfur MTBE by a rectification method and can be used for blending national V gasoline.
Related patents in China already adopt a rectification method to reduce the sulfur content of MTBE (application number 200910018228.2), and the sulfur content is reduced from 1000ppm to 10ppm under the condition of a reflux ratio of 1-10. The method adopts a single-tower flow, operates under the condition that the reflux ratio is more than 1, and has the tower bottom temperature of 90-120 ℃. The method adopts single-tower rectification, and adopts steam heating for heating, so that the energy consumption is high. In order to solve the problem of energy consumption, an MTBE double-tower rectification desulfurization technology is adopted at present, in a method for removing high-boiling-point sulfides in methyl tert-butyl ether (application number 201210559717.0) disclosed in the invention patent of 2014, the double-tower rectification desulfurization technology is adopted, MTBE desulfurization is carried out on a first tower at a lower temperature (the tower bottom temperature is 58-62 ℃), and an MTBE product with the sulfur content of 2-3ppm is obtained from the tower top. And recovering the MTBE in the first tower tailing in the second tower at a higher temperature (the tower bottom temperature is 75-95 ℃), and obtaining an MTBE product with the content of 3-5 ppm from the tower top. The MTBE product with the sulfur content lower than 5ppm is obtained after the first tower product and the second tower product are mixed. The double column rectification scheme was also used in the utility model 'a desulfurization unit for sulfur-containing methyl tert-butyl ether product' (application No. 201420873941.1) published in 2015, in which process column B is actually the stripping section of column a, and finally an MTBE product with sulfur content reduced to below 5ppm was obtained. The second column of both processes recovers only MTBE without consideration for the recovery of other high octane oxygenates. In the invention patent 'a device and a method for removing disulfide in methyl tert-butyl ether' (application number 201210065730.0) disclosed in 2014, after low-sulfur diesel oil and methyl tert-butyl ether are fully mixed according to the ratio of 1:1, the disulfide in the methyl tert-butyl ether is extracted into the low-sulfur diesel oil due to the principle of similar phase and dissolution, and then the low-sulfur MTBE is obtained by rectification.
Disclosure of Invention
The invention aims to provide a method and a device for desulfurizing methyl tert-butyl ether so as to better treat high-sulfur methyl tert-butyl ether.
In order to achieve the above object, according to one aspect of the present invention, there is provided a method for desulfurizing methyl t-butyl ether. The method adopts a double-tower rectification process, wherein the double towers comprise a rectification tower A and a rectification tower B, the rectification tower A is a desulfurization tower, and the rectification tower B is an oxygen-containing compound recovery tower.
Further, tail materials at the bottom of the tower, desulfurized by the rectification tower A, of the raw material methyl tert-butyl ether are used as main raw materials of the rectification tower B, the main raw materials are mixed with a diluent to obtain the raw materials of the rectification tower B, wherein the diluent is toluene and/or reformed gasoline, and the mass ratio of the main raw materials to the diluent is 1: 0.5-1.
Further, the temperature of the tower kettle of the rectification tower A is 56-65 ℃, the temperature of the tower top is 50-60 ℃, and the reflux ratio is 0.3-1.
Furthermore, the number of theoretical plates of the rectification tower B is 40-70, and the feed inlet is positioned in the middle of the rectification tower B.
Further, the temperature of the bottom of the rectification tower B is 110-130 ℃, the temperature of the top of the rectification tower B is 70-80 ℃, and the reflux ratio is 5-6.
Further, materials on the top of the rectification tower A and materials on the top of the rectification tower B are mixed to obtain a finished product of methyl tert-butyl ether with the sulfur content of 3-5 ppm.
According to another aspect of the present invention, there is provided an apparatus for desulfurizing methyl t-butyl ether. The device comprises a rectification tower A and a rectification tower B which are sequentially communicated, wherein the rectification tower A is a desulfurization tower, and the rectification tower B is an oxygen-containing compound recovery tower.
Furthermore, a mixer is arranged on a passage of the rectification tower A and the rectification tower B, and the mixer is provided with a diluent inlet.
Furthermore, the number of theoretical plates of the rectification tower B is 40-70, and the feed inlet is positioned in the middle of the rectification tower B.
And further, the system also comprises a finished product tank, and the finished product tank is communicated with material outlets at the top of the rectification tower A and the rectification tower B.
By applying the technical scheme of the invention, the double towers comprise a rectification tower A and a rectification tower B, the rectification tower A is a desulfurization tower, the rectification tower B is an oxygen-containing compound recovery tower, and the rectification tower B recovers the oxygen-containing compound which is a high-quality gasoline component and has considerable recovery value. Meanwhile, the technical problem that the tail material is treated by a gasoline and diesel oil hydrogenation mode, and the service life of a hydrogenation catalyst is influenced because water is generated in the hydrogenation process of the oxygen-containing compound is solved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
FIG. 1 shows a schematic diagram of the structure and flow of a methyl t-butyl ether desulfurization device according to an embodiment of the present invention.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
Both of the prior art patents identified under application numbers 201210559717.0 and 201420873941.1 are directed to the recovery of MTBE. The inventor finds that the tower bottom material of the tower usually contains oxygen-containing compounds such as tertiary butyl alcohol, secondary butyl alcohol, methyl tertiary amyl ether and the like besides MTBE, and the oxygen-containing compounds have higher octane number, are high-quality gasoline components and have considerable recovery value. In addition, for environmental protection, the two-tower tailing is generally treated by a gasoline hydrogenation method, but oxygen-containing compounds which are not recovered in the material can generate water in the hydrogenation process to poison a hydrogenation catalyst, so that the service life of the hydrogenation catalyst is influenced. It is therefore necessary to recover oxygenates other than MTBE in the tailings, both to obtain good quality gasoline components and to prevent catalyst poisoning.
According to an exemplary embodiment of the present invention, a method for the desulfurization of methyl tertiary butyl ether is provided. The method adopts a double-tower rectification process, wherein the double towers comprise a rectification tower A and a rectification tower B, the rectification tower A is a desulfurization tower, and the rectification tower B is an oxygen-containing compound recovery tower.
By applying the technical scheme of the invention, the double towers comprise a rectification tower A and a rectification tower B, the rectification tower A is a desulfurization tower, the rectification tower B is an oxygen-containing compound recovery tower, and the rectification tower B recovers the oxygen-containing compound which is a high-quality gasoline component and has considerable recovery value. Meanwhile, the technical problem that the tail material is treated by a gasoline and diesel oil hydrogenation mode, and the service life of a hydrogenation catalyst is influenced because water is generated in the hydrogenation process of the oxygen-containing compound is solved.
In addition, the inventor finds that in the prior art, the temperature of the bottom of the two towers is relatively high and is generally higher than 100 ℃. Rectification at a relatively high temperature causes decomposition of high-boiling sulfides to produce low-boiling sulfides such as methyl mercaptan and methyl sulfide. The boiling point of the sulfide is low, and the sulfide enters an MTBE product in the rectification process, so that the sulfur content of the MTBE product exceeds the standard. Inhibition of decomposition of high boiling sulfides at high temperatures is also an important issue in the rectification desulfurization of MTBE.
In order to solve the technical problem, the inventor finds that the means for inhibiting the decomposition can be solved by reducing the concentration and residence time of reactants, so that a proper diluent can be added into the feed of the rectification B tower to reduce the residence time of the macromolecular sulfide at the tower bottom so as to solve the decomposition problem, thereby further reducing the sulfur content of the MTBE product. In the patent application No. 201210065730.0 mentioned in the background, the desulfurization of low sulfur diesel fuel by blending it with high sulfur MTBE results in increased energy consumption due to the higher boiling point of the diesel fuel. In addition, the excessive temperature of the tower kettle can also promote the decomposition of the sulfide to be intensified. And the toluene or reformed gasoline is used as a raw material produced by a refinery, has a lower boiling point and can better play a role in inhibiting decomposition. And no adverse effect is generated in the tail material recovery and gasoline hydrogenation process. Thus toluene or reformed gasoline is used as diluent.
According to a typical embodiment of the invention, tail materials at the bottom of a rectification tower B after desulfurization of a raw material methyl tert-butyl ether through a rectification tower A are used as main raw materials of the rectification tower B, and the main raw materials are mixed with a diluent to obtain the raw materials of the rectification tower B, wherein the diluent is toluene and/or reformed gasoline, and the mass ratio of the main raw materials to the diluent is 1: 0.5-1. The diluent is an internal raw material of a refinery, can not be introduced from the outside, and does not influence the treatment of tailings. The rectification tower A is used as a desulfurizing tower, and can remove sulfides in high-sulfur MTBE with lower energy consumption. A reboiler heat source of the rectification A tower adopts a low-temperature heat source, preferably, the temperature of a tower kettle of the rectification A tower is 56-65 ℃, the temperature of a tower top is 50-60 ℃, and the reflux ratio is 0.3-1. In a specific embodiment of the invention, the MTBE product with the sulfur content of 2-3ppm is obtained at the top of the rectifying tower A, the sulfur content of 10000-20000ppm is obtained at the bottom of the rectifying tower A, and the content of the oxide is 30-60%.
According to a typical embodiment of the invention, the number of theoretical plates of the rectification tower B is 40-70, and the feed inlet is positioned in the middle of the rectification tower B. Preferably, the tower bottom temperature of the rectification B tower is 110-130 ℃, the tower top temperature is 70-80 ℃, and the reflux ratio is 5-6. In a specific embodiment of the invention, a product mainly containing oxygen-containing compounds such as MTBE, tert-butyl alcohol and methyl tert-amyl ether is obtained from the top of a rectifying tower B, and the sulfur content is 50-100 ppm.
According to a typical embodiment of the invention, materials at the top of the rectification tower A and the rectification tower B are mixed to obtain a finished product of methyl tert-butyl ether with the sulfur content of 3-5 ppm, and the finished product of methyl tert-butyl ether can be used for gasoline blending. The content of high-octane oxygenates in the bottom material of the rectifying tower B is less than 1 percent.
According to a typical embodiment of the invention, a double-tower rectification process is adopted, wherein the rectification A tower is used as a desulfurization tower, and sulfides in high-sulfur MTBE are removed with lower energy consumption. The raw material of the rectification A tower is high-sulfur MTBE, a reboiler heat source of the rectification A tower adopts a low-temperature heat source, the temperature of a tower kettle of the rectification A tower is 56-65 ℃, the temperature of a tower top is 50-60 ℃, and the reflux ratio is 0.3-1. The MTBE product with the sulfur content of 2-3ppm is obtained at the top of the rectifying tower A, and the sulfur content and the oxide content of 10000-20000ppm and 30-60% are obtained at the bottom of the rectifying tower A. The rectification column B is used as an oxygenate recovery column to recover high-octane oxygenates such as MTBE, tert-butyl alcohol, methyl tert-amyl ether and the like. And the rectification B tower takes the bottom material of the rectification A tower as a main raw material, and takes methylbenzene or reformed gasoline as a diluent to reduce the concentration of macromolecular sulfides, so that the decomposition of the macromolecular sulfides is inhibited. The two are mixed to be used as a raw material of a rectification B tower, the raw material is heated by a reboiler, the temperature of the bottom of the tower is 110-130 ℃, the temperature of the top of the tower is 70-80 ℃, and the reflux ratio of the top of the tower is 5-6. And (3) obtaining a product mainly containing oxygen-containing compounds such as MTBE, tert-butyl alcohol, methyl tert-amyl ether and the like from the tower top, wherein the sulfur content is 50-100 ppm, and mixing the product with the product at the tower top of the rectification tower A to obtain a finished product MTBE with the sulfur content of 3-5 ppm, and the finished product MTBE is used for gasoline blending. The content of high-octane oxygenates in the bottom material of the rectification tower B is lower than 1 percent, and the full recovery of the oxygenates is ensured. The tower bottom material can be mixed with refinery gasoline hydrogenation raw materials and finally returned to gasoline blending components.
According to an exemplary embodiment of the present invention, an apparatus for desulfurizing methyl tertiary butyl ether is provided. The device comprises a rectification tower A and a rectification tower B which are sequentially communicated, wherein the rectification tower A is a desulfurization tower, and the rectification tower B is an oxygen-containing compound recovery tower.
By applying the technical scheme of the invention, the double towers comprise a rectification tower A and a rectification tower B, the rectification tower A is a desulfurization tower, the rectification tower B is an oxygen-containing compound recovery tower, and the rectification tower B recovers the oxygen-containing compound which is a high-quality gasoline component and has considerable recovery value. Meanwhile, the technical problem that the tail material is treated by adopting a gasoline hydrogenation mode, and the service life of a hydrogenation catalyst is influenced because water is generated in the hydrogenation process of the oxygen-containing compound is solved.
According to a typical embodiment of the invention, a mixer is arranged on the path of the rectification A tower and the rectification B tower, and the mixer is provided with a diluent inlet. And a diluent inlet is used for inputting a diluent into the mixer, and the diluent and tower bottom tailings desulfurized by the rectification tower A are mixed in the mixer to be used as a main raw material of the rectification tower B.
Preferably, the number of theoretical plates of the rectification tower B is 40-70, and the feed inlet is positioned in the middle of the rectification tower B.
According to a typical embodiment of the invention, the system further comprises a finished product tank, and the finished product tank is communicated with the material outlets at the top of the rectification tower A and the rectification tower B. And mixing the materials at the top of the rectification A tower and the materials at the top of the rectification B tower to obtain a finished product of methyl tertiary butyl ether with the sulfur content of 3-5 ppm, wherein the finished product of methyl tertiary butyl ether can be used for gasoline blending.
The following examples are provided to further illustrate the advantageous effects of the present invention.
As shown in fig. 1, a tower a condenser 3 and a tower a reflux tank 6 connected in series are arranged at the top of a tower a 2 of rectification, a tower a reboiler 4 is arranged at the bottom, a tower B condenser 12 and a tower B reflux tank 15 connected in series are arranged at the top of a tower B9 of rectification, a tower B reboiler 13 is arranged at the bottom, a material outlet at the bottom of the tower a 2 of rectification is communicated with a material inlet at the middle of the tower B of rectification, and a mixer 7 is further arranged on a communicating pipeline. In addition, the product of the A tower condenser 3 returns to the rectification A tower 2 and is sent to a finished product tank 19 respectively, the product of the B tower condenser 15 returns to the rectification B tower 9 and is sent to the finished product tank 19 respectively, and the bottom material outlet of the rectification B tower 9 is communicated with a B tower tail material tank 17.
As shown in figure 1, high-sulfur MTBE 1 enters a rectification tower A2, tower bottom tailing 5 desulfurized by the rectification tower A is mixed with a diluent 8 in a mixer 7 to be used as a raw material 10 of a rectification tower B9, and a finished product of methyl tert-butyl ether 18 obtained after a tower top material 11 of the rectification tower A2 and a tower top material 16 of the rectification tower B9 are mixed enters a finished product tank 19. The tower bottom material 14 of the rectification B tower 9 enters a B tower tail material tank 17.
In all the following embodiments, the number of theoretical plates of the rectification column B is 60, the feed inlet is positioned in the middle of the rectification column B, the raw materials of the rectification column A are high-sulfur MTBE, the temperature of the bottom of the rectification column A is 56-65 ℃, the temperature of the top of the rectification column A is 56-65 ℃, and the reflux ratio is 0.3-1.
Example 1
And in the rectification B tower, the bottom material of the rectification A tower is used as a main raw material, the toluene is used as a diluent, and the two materials are mixed to be used as a raw material. The mixing ratio of the main raw material to the diluent is 1:0.8 (m/m). At this time, the content of the oxygen-containing compound in the raw material was 30.34% and the sulfur content was 7800 ppm. The raw materials enter a rectifying tower from the middle part and are heated by a reboiler, the temperature at the bottom of the tower ranges from 110 ℃ to 115 ℃, the temperature at the top of the tower ranges from 75 ℃ to 80 ℃, the reflux ratio is 6, and the test time of the embodiment is 70 hours.
Example 2
And in the rectification B tower, the bottom material of the rectification A tower is used as a main raw material, the toluene is used as a diluent, and the two materials are mixed to be used as a raw material. The mixing ratio of the main raw material to the diluent is 1:1 (m/m). At this time, the concentration of the oxygen-containing compound in the feed was 23.65% (m/m), and the sulfur content was 6250 ppm. The raw materials enter a rectifying tower from the middle part and are heated by a reboiler, the tower bottom temperature is 115-125 ℃, the tower top temperature is 78-80 ℃, the reflux ratio is 6, and the test time of the embodiment is 60 hours.
Example 3
And the rectification tower B takes the tower bottom material of the rectification tower A as a main raw material, reformed gasoline as a diluent, and the two are mixed to serve as a raw material. The mixing ratio of the main raw material to the diluent is 1:0.7 (m/m). At this time, the concentration of the oxygen-containing compound in the feed was 21.34% (m/m), and the sulfur content was 8054 ppm. The raw materials enter a rectifying tower from the middle part and are heated by a reboiler, the temperature at the bottom of the tower ranges from 120 ℃ to 130 ℃, the temperature at the top of the tower ranges from 75 ℃ to 80 ℃, the reflux ratio is 6, and the test time of the embodiment is 60 hours.
Example 4
And the rectification tower B takes the tower bottom material of the rectification tower A as a main raw material, reformed gasoline as a diluent, and the two are mixed to serve as a raw material. The mixing ratio of the main raw material to the diluent is 1:1 (m/m). At this time, the content of the oxygen-containing compound in the feed was 17.55% (m/m), and the sulfur content was 7853 ppm. The raw materials enter a rectifying tower from the middle part and are heated by a reboiler, the temperature at the bottom of the tower ranges from 120 ℃ to 130 ℃, the temperature at the top of the tower ranges from 75 ℃ to 80 ℃, the reflux ratio is 6, and the test time of the embodiment is 70 hours.
Example 5
And the rectification tower B takes the tower bottom material of the rectification tower A as a main raw material, reformed gasoline as a diluent, and the two are mixed to serve as a raw material. The mixing ratio of the main raw material to the diluent is 1:1 (m/m). At this time, the content of the oxygen-containing compound in the feed was 17.55% (m/m), and the sulfur content was 7853 ppm. The raw materials enter a rectifying tower from the middle part and are heated by a reboiler, the temperature at the bottom of the tower ranges from 120 ℃ to 130 ℃, the temperature at the top of the tower ranges from 73 ℃ to 80 ℃, the reflux ratio is 5, and the test time of the embodiment is 30 hours.
Example 6
And the rectification tower B takes the tower bottom material of the rectification tower A as a main raw material, reformed gasoline as a diluent, and the two are mixed to serve as a raw material. The mixing ratio of the main raw material to the diluent is 1:0.5 (m/m). At this time, the content of the oxygen-containing compound in the feed was 25.31% (m/m), and the sulfur content was 8964 ppm. The raw materials enter a rectifying tower from the middle part and are heated by a reboiler, the temperature at the bottom of the tower ranges from 120 ℃ to 130 ℃, the temperature at the top of the tower ranges from 75 ℃ to 80 ℃, the reflux ratio is 6, and the test time of the embodiment is 60 hours.
The relevant experimental parameters in the above examples are shown in table 1.
TABLE 1
Figure BDA0001189053770000061
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
the method comprises the steps of adopting a double-tower rectification process, taking high-sulfur MTBE as a rectification A tower raw material, taking a rectification A tower as a desulfurizing tower, taking a low-temperature heat source as a heating source, carrying out rectification desulfurization at a low temperature, and obtaining low-sulfur MTBE with the sulfur content of 2-3ppm from the top of the tower. And the tail material at the bottom of the rectification A tower is used as a main raw material of a rectification B tower, reformed high-octane gasoline or toluene is added as a diluent to inhibit the decomposition of high-boiling-point sulfides, the two are mixed to be used as a raw material of the rectification B tower, after oxides are rectified and recovered by the rectification B tower, a product mainly containing high-octane oxygen-containing compounds such as MTBE, tert-butyl alcohol, methyl tert-amyl ether and the like is obtained from the tower top, the sulfur content is less than 100ppm, the product is mixed with low-sulfur MTBE at the tower top of the rectification A tower to obtain an MTBE finished product with the sulfur content of 3-5 ppm, the component can be directly used as a gasoline blending component, and a small amount of non-condensable gas at the tower top is discharged into a low-pressure gas system. The content of high-octane oxygenates in the bottom material of the rectification tower B is lower than 1 percent, and the full recovery of the oxygenates is ensured. The bottom material can be mixed with refinery gasoline hydrogenation raw material, the main part returns gasoline blending component, the hydrocarbon composition has almost no loss, sulfur is absorbed by amine in the form of hydrogen sulfide, and finally sulfur is recovered in the form of sulfur. The non-condensable gas at the tower top enters a thermoelectric system along with low-pressure gas, and sulfides are removed in a flue gas desulfurization device, so that the environmental problem is avoided.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (2)

1. A method for desulfurizing methyl tert-butyl ether adopts a double-tower rectification process, the double towers comprise a rectification tower A and a rectification tower B, and the method is characterized in that the rectification tower A is a desulfurization tower, the rectification tower B is an oxygen-containing compound recovery tower,
taking tower bottom tailing of a raw material methyl tert-butyl ether desulfurized by the rectification tower A as a main raw material of the rectification tower B, mixing the main raw material with a diluent to obtain the raw material of the rectification tower B, wherein the diluent is toluene and/or reformed gasoline, the mass ratio of the main raw material to the diluent is 1: 0.5-1,
the temperature of the tower kettle of the rectification tower A is 56-65 ℃, the temperature of the tower top is 50-60 ℃, the reflux ratio is 0.3-1,
the number of theoretical plates of the rectification column B is 40-70, the feed inlet is positioned in the middle of the rectification column B, and
the temperature of the bottom of the rectification tower B is 110-130 ℃, the temperature of the top of the rectification tower B is 70-80 ℃, and the reflux ratio is 5-6.
2. The method according to claim 1, wherein the top materials of the rectification A tower and the rectification B tower are mixed to obtain a finished product of methyl tert-butyl ether with the sulfur content of 3-5 ppm.
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Citations (4)

* Cited by examiner, † Cited by third party
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CN102557888A (en) * 2011-12-23 2012-07-11 中国石油大学(北京) Method for deeply desulfurizing methyl tertiary butyl ether
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