CN209797875U - High-yield MTBE catalytic distillation device - Google Patents
High-yield MTBE catalytic distillation device Download PDFInfo
- Publication number
- CN209797875U CN209797875U CN201920187946.1U CN201920187946U CN209797875U CN 209797875 U CN209797875 U CN 209797875U CN 201920187946 U CN201920187946 U CN 201920187946U CN 209797875 U CN209797875 U CN 209797875U
- Authority
- CN
- China
- Prior art keywords
- mtbe
- tower
- catalytic distillation
- distillation tower
- methanol
- 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.)
- Active
Links
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A high-yield MTBE catalytic distillation device relates to the technical field of MTBE distillation, hydrogen sulfide and light components generated by the reaction of liquefied gas after etherification are distilled to the top of a catalytic distillation tower, the hydrogen sulfide and the light components enter a stripping tower after being condensed by a first condenser, one part of the hydrogen sulfide and the light components enter a reduction washing tank as a tower top product, tail gas containing the hydrogen sulfide is discharged after the hydrogen sulfide is absorbed by the reduction washing tank, the yield of MTBE is preliminarily improved, a first feed inlet on the side wall of an MTBE re-catalytic distillation tower is connected with a discharge outlet at the top of an extraction tower, so as to lead the unreacted C4 in the second distillation tower to enter the MTBE re-catalytic distillation tower, the feed inlet of the methanol feed pump is communicated with the methanol outlet of the methanol tower, the discharge hole of the methanol feed pump is communicated with the methanol inlet of the MTBE catalytic distillation tower, so that the unreacted methanol enters the reaction section of the MTBE catalytic distillation tower and continuously reacts with C4 to generate MTBE, and the yield of the MTBE is improved.
Description
Technical Field
The utility model relates to a MTBE distills technical field, in particular to high yield MTBE catalytic distillation unit.
Background
MTBE is an abbreviation of methyl tertiary butyl ether, melting point is-109 ℃, boiling point is 55.2 ℃, is colorless, transparent and high-octane liquid, has ether-like smell, is an ideal blending component for producing lead-free, high-octane and oxygen-containing gasoline, and is widely used as a gasoline additive all over the world. It can not only effectively increase the octane number of gasoline, but also improve the performance of automobiles, reduce the content of CO in exhaust gas and reduce the production cost of gasoline. In addition, MTBE is an important chemical raw material, and high-purity isobutene can be prepared by cracking. MTBE is an organic ether with an oxygen content of 18.2%.
Along with the increasingly strict requirement on environmental protection, the restriction on the sulfur content in the motor gasoline by countries in the world is more and more strict, the MTBE has higher solubility on sulfides than the carbon tetrahydrocarbon in the production process of the MTBE, and the boiling point of most sulfides is higher than that of the carbon tetrahydrocarbon, so that most sulfides in the feed carbon tetrahydrocarbon are enriched in the MTBE product, the sulfur content of the MTBE product is high, and therefore, how to reduce the sulfur content in the motor gasoline is a major subject currently faced;
In addition, the MTBE mainly takes oil refining liquefied gas mixed carbon four and industrial methanol as raw materials, and most sulfides in the liquefied gas carbon four are enriched in the MTBE, so that the conversion rate of isobutene in the carbon four before ether produced by an expansion bed reactor which takes the oil refining mixed carbon four as a raw material is low, the conversion rate of isobutene is about 90% generally, isobutene in the carbon four before ether cannot completely react, a part of isobutene components are wasted, excessive methanol cannot completely participate in the reaction to cause that tetramethyl alcohol after ether exceeds the standard, influences are brought to the production and product quality of downstream devices, and most importantly, the yield of the MTBE product is influenced, the enterprise income is reduced, and the enterprise operation cost is increased.
Disclosure of Invention
In view of the above, there is a need for a high-yield MTBE catalytic distillation apparatus that reduces the sulfur content in motor gasoline and increases the yield of MTBE product.
The high-yield MTBE catalytic distillation device comprises a catalytic distillation hydrodesulfurization device and an MTBE re-reaction device, wherein a discharge hole of the catalytic distillation hydrodesulfurization device is connected with a feed hole of the MTBE re-reaction device, so that low-yield MTBE, unreacted C4 and methanol in the catalytic distillation hydrodesulfurization device are re-reacted through the MTBE re-reaction device to obtain high-yield MTBE; the catalytic distillation hydrodesulfurization device comprises an etherification reactor, a first distillation tower, a second distillation tower, a catalytic distillation tower, a first condenser, a stripping tower, an alkaline washing tank, a gate valve, a reflux pump, a second condenser, an extraction tower and a methanol tower, wherein an outlet of the etherification reactor is connected with an inlet of the first distillation tower, an outlet of the bottom of the first distillation tower is connected with an inlet of the second distillation tower, an outlet of the bottom of the second distillation tower is connected with an inlet in the middle of the catalytic distillation tower, a hydrogen inlet is further arranged at the lower part of the catalytic distillation tower, an outlet of the top of the second distillation tower is connected with an inlet of the first condenser, an outlet of the first condenser is connected with an inlet of the stripping tower, an outlet of the top of the stripping tower is connected with an inlet of the alkaline washing tank, a gate valve is arranged on a discharge pipeline at an outlet of the bottom of the stripping tower, an inlet of the reflux pump is communicated with, the outlet of the reflux pump is connected with a reflux port at the middle upper part of the catalytic distillation tower, the outlet at the bottom of the catalytic distillation tower is connected with the inlet of the second condenser, the outlet at the top of the first distillation tower is connected with the inlet of the extraction tower, and the outlet at the bottom of the extraction tower is connected with the inlet of the methanol tower; the MTBE re-reaction device comprises an MTBE re-catalytic distillation tower, a methanol feed pump, a reboiler, a product pump, an MTBE finished product tank and a gas separation device header pipe, a first feed port in the side wall of the MTBE re-catalytic distillation tower is connected with a discharge port in the top of the extraction tower so as to enable unreacted C4 in the extraction tower to enter the MTBE re-catalytic distillation tower, a feed port of the methanol feed pump is communicated with a methanol outlet of the methanol tower, and a discharge port of the methanol feed pump is communicated with a methanol inlet of the MTBE catalytic distillation tower so as to enable methanol in the methanol tower to enter the MTBE catalytic distillation tower and react with C4 to generate MTBE continuously; the first discharge gate of MTBE re-catalytic distillation tower bottom is connected with the feed inlet of reboiler bottom to let the liquid phase thing of bottom in the tower naturally flow into the reboiler through gravity, the discharge gate and the MTBE re-catalytic distillation tower on the near lateral wall of bottom of reboiler top are connected, so that let the fluid after the heating get into the MTBE re-catalytic distillation tower, the second discharge gate and the feed inlet of product pump of MTBE re-catalytic distillation tower bottom are connected, so that go into the fluid pump of bottom in the tower product pump, the discharge gate of product pump is connected with the feed inlet of MTBE finished product jar, so that go into the fluid pump of bottom in the tower MTBE finished product jar, the gas outlet of gas-devided main pipe is connected with the bottom of MTBE re-catalytic distillation tower, lets in nitrogen gas, low pressure steam to the MTBE re-catalytic distillation tower.
Preferably, the MTBE re-reaction device further comprises an underground sump oil tank, and a feed inlet of the underground sump oil tank is connected with the bottom of the MTBE re-catalytic distillation tower, so that sump oil enters the underground sump oil tank.
Preferably, the MTBE re-catalytic distillation tower includes stripping section, reaction section, rectification section, the stripping section is located the tower lower part, be equipped with the float valve tray in the stripping section, the reaction section is located the tower middle part, the reaction section is equipped with several sections reaction bed layers, all is provided with cyclic annular grid on every reaction bed layer, bale formula hydrogen type acid ion exchange resin catalyst is equipped with in the cyclic annular grid, the rectification section is located tower upper portion, be equipped with regular packing and float valve tray in the rectification section.
Preferably, the catalytic distillation hydrodesulfurization device further comprises a microprocessor, and a mass flow meter and a flow meter which are connected with the microprocessor, wherein the mass flow meter is installed on a pipeline between an outlet at the bottom of the first distillation tower and an inlet of the second distillation tower, the flow meter is installed on a pipeline at an outlet at the top of the second distillation tower, the mass flow meter is used for controlling the feeding amount entering the second distillation tower, the flow meter is used for detecting the extraction amount of the second distillation tower in real time, the microprocessor calculates according to a pre-stored algorithm according to the detection extraction amount of the flow meter, and feeds back the calculation result to the mass flow meter so as to control the feeding amount of the second distillation tower through the mass flow meter.
Preferably, the algorithm prestored in the microprocessor is to calculate the produced quantity by substituting the produced quantity into the following formula, and then calculate the feeding quantity, wherein D/F = A, and D is the produced quantity and has the unit of cubic meter per hour; f is the feeding amount and the unit is cubic meter per hour; a is a constant.
The beneficial effects of the utility model reside in that: according to the scheme, liquefied gas after etherification is distilled by a first distillation tower and a second distillation tower to remove high-boiling-point sulfides from MTBE, low-sulfur MTBE is distilled out from the top of the second distillation tower, high-sulfur MTBE is discharged from the bottom of the second distillation tower and then is conveyed into a catalytic distillation tower from the middle part of the catalytic distillation tower, hydrogen sulfide and light components generated by reaction are distilled to the top of the catalytic distillation tower, the hydrogen sulfide and the light components enter a stripping tower after being condensed by a first condenser, one part of stripped liquid is refluxed, the other part of stripped liquid enters an alkaline washing tank as a tower top product, and tail gas containing hydrogen sulfide is discharged after absorbing the hydrogen sulfide by the alkaline washing tank, so that the low-sulfur MTBE is obtained, the sulfur content in the high-sulfur MTBE is reduced, and the yield of the MTBE is preliminarily improved; the first feed inlet on the side wall of the MTBE re-catalytic distillation tower is connected with the discharge outlet at the top of the extraction tower so as to enable unreacted C4 in the extraction tower to enter the MTBE re-catalytic distillation tower, the feed inlet of the methanol feed pump is communicated with the methanol outlet of the methanol tower, and the discharge outlet of the methanol feed pump is communicated with the methanol inlet of the MTBE catalytic distillation tower, so that methanol enters the MTBE catalytic distillation tower to react with C4 to generate MTBE, and the yield of the MTBE is improved.
Drawings
Fig. 1 is a schematic structural diagram of the high-yield MTBE catalytic distillation apparatus.
In the figure: the high-yield MTBE catalytic distillation device 10, the catalytic distillation hydrodesulfurization device 20, the etherification reactor 21, the first distillation tower 22, the second distillation tower 23, the catalytic distillation tower 24, the first condenser 25, the stripping tower 26, the caustic wash tank 27, the gate valve 28, the reflux pump 29, the second condenser 210, the extraction tower 211, the methanol tower 212, the MTBE re-reaction device 30, the MTBE re-catalytic distillation tower 31, the reboiler 32, the product pump 33, the MTBE finished product tank 34, the gas separation device header 35, the methanol feed pump 36, the underground sump tank 37, the mass flow meter 40 and the flow meter 50.
Detailed Description
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without creative efforts.
Referring to fig. 1, the embodiment of the present invention provides a high-yield MTBE catalytic distillation apparatus 10, including catalytic distillation hydrodesulfurization unit 20 and MTBE re-reaction unit 30, a discharge port of catalytic distillation hydrodesulfurization unit 20 is connected to a feed port of MTBE re-reaction unit 30, so as to re-react low-yield MTBE, unreacted C4, and methanol in catalytic distillation hydrodesulfurization unit 20 through MTBE re-reaction unit 30 to obtain high-yield MTBE; the catalytic distillation hydrodesulfurization device 20 comprises an etherification reactor 21, a first distillation tower 22, a second distillation tower 23, a catalytic distillation tower 24, a first condenser 25, a stripping tower 26, a caustic wash tank 27, a gate valve 28, a reflux pump 29, a second condenser 210, an extraction tower 211 and a methanol tower 212, wherein an outlet of the etherification reactor 21 is connected with an inlet of the first distillation tower 22, an outlet at the bottom of the first distillation tower 22 is connected with an inlet of the second distillation tower 23, an outlet at the bottom of the second distillation tower 23 is connected with an inlet at the middle part of the catalytic distillation tower 24, a hydrogen inlet is further arranged at the lower part of the catalytic distillation tower 24, an outlet at the top of the second distillation tower 23 is connected with an inlet of the first condenser 25, an outlet of the first condenser 25 is connected with an inlet of the stripping tower 26, an outlet at the top of the stripping tower 26 is connected with an inlet of the caustic wash tank 27, a discharge pipeline at an outlet, an inlet of the reflux pump 29 is communicated with a discharge pipeline, a joint of the reflux pump 29 and the discharge pipeline is positioned between an outlet at the bottom of the stripping tower 26 and the gate valve 28, an outlet of the reflux pump 29 is connected with a reflux port at the middle upper part of the catalytic distillation tower 24, an outlet at the bottom of the catalytic distillation tower 24 is connected with an inlet of the second condenser 210, an outlet at the top of the first distillation tower 22 is connected with an inlet of the extraction tower 211, and an outlet at the bottom of the extraction tower 211 is connected with an inlet of the methanol tower 212; the MTBE re-reaction device 30 comprises an MTBE re-catalytic distillation tower 31, a methanol feed pump 36, a reboiler 32, a product pump 33, an MTBE finished product tank 34, and a gas separation device header 35, a first feed port on a side wall of the MTBE re-catalytic distillation tower 31 is connected with a discharge port on the top of the extraction tower 211 to feed unreacted C4 in the extraction tower 211 into the MTBE re-catalytic distillation tower 31, a feed port of the methanol feed pump 36 is communicated with a methanol outlet of the methanol tower 212, and a discharge port of the methanol feed pump 36 is communicated with a methanol inlet of the MTBE catalytic distillation tower 24 to enable methanol in the methanol tower 212 to enter the MTBE catalytic distillation tower 24 to react with C4 to generate MTBE; the first discharge hole at the bottom end of the MTBE re-catalytic distillation tower 31 is connected with the feed inlet at the bottom end of the reboiler 32, so that the liquid phase substance at the bottom in the tower naturally flows into the reboiler 32 by gravity, the discharge hole at the top end of the reboiler 32 is connected with the second feed hole on the side wall near the bottom end of the MTBE re-catalytic distillation tower 31, so that the heated fluid enters the MTBE re-catalytic distillation tower 31, the second discharge hole at the bottom end of the MTBE re-catalytic distillation tower 31 is connected with the feed inlet of the product pump 33, so that the fluid at the bottom in the tower is pumped into the product pump 33, the discharge hole of the product pump 33 is connected with the feed inlet of the MTBE finished product tank 34, so that the fluid at the bottom in the tower is pumped into the MTBE finished product tank 34, and the gas outlet of the gas separator header 35 is connected with the bottom of the MTBE re-catalytic distillation tower 31, so that.
An air inlet at the upper end of the reboiler 32 is connected with one end of the steam main pipe to absorb steam of the steam main pipe and utilize heat in the steam, and a liquid outlet at the lower end of the reboiler 32 is connected with one end of the condensed water main pipe to discharge condensed water cooled by the exothermic reaction.
The reboiler 32 is a special heat exchanger that can exchange heat while having a vaporization space. The feed level in reboiler 32 and the MTBE re-catalytic distillation column 31 level are at the same height. The liquid phase is provided from the bottom line into reboiler 32. Typically 25-30% of the liquid phase is vaporized in reboiler 32. The vaporized two-phase stream is fed back to the fractionation column where the C4 and methanol pass upward through trays and the liquid phase component MTBE falls back to the bottom of the column. The material expands and even vaporizes in the reboiler 32 due to heat, and the density of the material decreases, so that the material leaves the vaporization space, and the liquid level in the bottom of the tower is continuously replenished due to the static pressure difference. The reboiler 32 vaporizes the heavy component in the liquid phase at the bottom of the rectifying tower, and the gas phase flows upwards and is partially vaporized and partially condensed with the light component liquid phase from the reflux tank for many times on the tower plate or the packing layer, so that the mixture is separated with high purity.
The beneficial effects of the utility model reside in that: in the scheme, liquefied gas after etherification is distilled by a first distillation tower 22 and a second distillation tower 23 to remove high-boiling-point sulfides from MTBE, low-sulfur MTBE is distilled from the top of the second distillation tower 23, high-sulfur MTBE is discharged from the bottom of the second distillation tower 23 and then is conveyed into a catalytic distillation tower 24 from the middle part of the catalytic distillation tower 24, hydrogen sulfide and light components generated by reaction are distilled to the top of the catalytic distillation tower 24, the hydrogen sulfide and light components are condensed by a first condenser 25 and then enter a stripping tower 26, one part of stripped liquid is refluxed, the other part of stripped liquid is taken as a tower top product and enters an alkaline tank 27, and tail gas containing hydrogen sulfide is discharged after absorbing hydrogen sulfide by the alkaline tank 27, so that low-sulfur MTBE is obtained, the sulfur content in high-MTBE is reduced, and the yield of MTBE is initially improved; the first feed inlet on the side wall of the MTBE re-catalytic distillation tower 31 is connected with the discharge outlet on the top of the extraction tower 211 so as to feed the unreacted C4 in the extraction tower 211 into the MTBE re-catalytic distillation tower, the feed inlet of the methanol feed pump 36 is communicated with the methanol outlet of the methanol tower 212, and the discharge outlet of the methanol feed pump 36 is communicated with the methanol inlet of the MTBE catalytic distillation tower 31, so that the methanol in the methanol tower 212 enters the MTBE catalytic distillation tower 31 to react with the C4 to generate MTBE, and the yield of the MTBE is improved.
Further, the MTBE re-reaction device 30 further comprises an underground sump oil tank 36, and a feed inlet of the underground sump oil tank 36 is connected with the bottom of the MTBE re-catalytic distillation tower 31, so that sump oil enters the underground sump oil tank 36.
Further, the MTBE re-catalytic distillation tower 31 comprises a stripping section, a reaction section and a rectification section, wherein the stripping section is located at the lower part of the tower, a float valve tray is arranged in the stripping section, the reaction section is located at the middle part of the tower, the reaction section is provided with a plurality of reaction beds, each reaction bed is provided with an annular grid, a bundled hydrogen type acidic ion exchange resin catalyst is arranged in each annular grid, the rectification section is located at the upper part of the tower, and the rectification section is internally provided with regular packing and a float valve tray.
the utility model discloses utilize vertical multistage strip tower 26's energy-conserving technique to research and develop MTBE re-catalytic distillation tower 31, the technical characterstic of this tower is to combine reaction and product separation to go on in an equipment, because reaction and separation go on simultaneously, the destructive reaction is balanced, improves the conversion, shortens process flow, reduces the equipment investment, utilizes the reaction heat, reduces the energy consumption. MTBE is continuously separated and recombined in the tower, so that the reaction is advanced, and the isobutene achieves higher conversion rate.
The MTBE re-catalytic distillation tower 31 is hinged with switch doors at the positions of the stripping section, the reaction section and the rectification section respectively, and temperature-resistant sealing rubber rings are arranged in the switch doors. The bale hydrogen type acidic ion exchange resin catalyst consists of two metal wire nets and pipe-strip-shaped mesh bags arranged on the metal wire nets, the pipe-strip-shaped mesh bags are arranged in a staggered mode, and a gas-liquid distributor is arranged between every two adjacent reaction bed layers. The float valve tray is provided with two arched downcomers.
The stripping section is used for discharging and primarily evaporating MTBE, the reaction section is used for catalytically distilling gas generated by the MTBE, and the rectification section is used for distilling the catalyzed gas again, so that different distillation products are collected. The improved cavity distillation tower is characterized in that float valve trays are arranged in the stripping section, feed inlets are formed in the middle positions of all the float valve trays, inclined feed pipes are connected to the feed inlets, two arched downcomers are arranged on each float valve tray, a heating mechanism is arranged outside the cavity distillation tower body and can perform primary evaporation on the MTBE (methyl tert-butyl ether), the MTBE performs gas-liquid separation on the float valve trays in the middle positions at first, gas moves upwards from the bottom, liquid moves downwards from the float valve trays in the middle positions along the arched downcomers, and each float valve tray on the lower layer can perform gas-liquid separation, so that the distillation effect is improved, gas and liquid are completely separated, and the utilization rate of the MTBE is improved.
principle of float valve tray: the tray is provided with a plurality of holes, each hole is provided with a valve, when no ascending vapor phase exists, the floating valve is closed on the tray plate, when the vapor phase ascends, the floating valve is impacted by the vapor flow and is opened upwards, the opening degree is increased along with the increase of the amount of the vapor phase, the ascending vapor phase passes through the valve hole and is dispersed to the horizontal direction under the action of the floating valve plate, and the vapor phase and the liquid phase are fully contacted through bubbling of a liquid layer, so that the ideal heat and mass transfer effect is achieved.
Be equipped with the gas-liquid distributor between two adjacent reaction beds, annular grid can be fixed bale formula hydrogen type acidic ion exchange resin catalyst, guarantee in the reaction, the structure is firm, stable in structure, thereby increase catalytic distillation's effect, the gas-liquid distributor can improve the ability that the commodity circulation sweeps the catalyst, bed gas content and commodity circulation impact force are improved, thereby accelerate catalytic action, improve catalytic efficiency, the catalyst bale has the dual function of excellent catalytic reaction and product separation, it can be used to corresponding reaction process to pack into different types of catalyst in the subassembly, catalyzed gas can escape smoothly in the catalyst bale, thereby realize quick complete catalytic treatment. The gas-liquid distributor is a disc distributor formed by arranging and welding a plurality of distribution grooves in specification, and plays roles in collecting liquid, distributing gas and collecting lateral lines. The catalyst bale is made by a specially made wire mesh, placing a tubular strip-shaped mesh bag filled with resin catalyst on the wire mesh, winding and binding. The metal wire mesh used in the assembly is a stainless steel mesh which is woven according to specific requirements and pressed into an oblique corrugated shape; the semi-rigid tubular mesh bag filled with resin catalyst is a small bag made of two layers of high-permeability and corrosion-resistant fiber fabrics according to a certain warp and weft.
Further, the catalytic distillation hydrodesulfurization device 20 further comprises a microprocessor, and a mass flow meter 50 and a flow meter 60 connected with the microprocessor, wherein the mass flow meter 50 is installed on a pipeline between an outlet at the bottom of the first distillation tower 22 and an inlet of the second distillation tower 23, the flow meter 60 is installed on a pipeline at an outlet at the top of the second distillation tower 23, the mass flow meter 50 is used for controlling a feeding amount entering the second distillation tower 23, the flow meter 60 is used for detecting a produced amount of the second distillation tower 23 in real time, the microprocessor calculates according to a pre-stored algorithm according to the detected produced amount of the flow meter 60, and feeds back a calculation result to the mass flow meter 50 so as to control the feeding amount of the second distillation tower 23 through the mass flow meter 50.
Further, the algorithm prestored in the microprocessor is to calculate the produced quantity by substituting the produced quantity into the following formula, and then calculate the feeding quantity, wherein D/F = A, D is the produced quantity, and the unit is cubic meter per hour; f is the feeding amount and the unit is cubic meter per hour; a is a constant.
In the embodiment, only the relative stability of the feeding amount and the extraction amount needs to be kept, and the heating energy consumption of the second distillation tower 23 can be effectively reduced.
The embodiment of the utility model provides a module or unit in the device can merge, divide and delete according to actual need.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention.
Claims (3)
1. A high yield MTBE catalytic distillation unit which characterized in that: the device comprises a catalytic distillation hydrodesulfurization device and an MTBE re-reaction device, wherein a discharge hole of the catalytic distillation hydrodesulfurization device is connected with a feed hole of the MTBE re-reaction device, so that low-yield MTBE, unreacted C4 and methanol in the catalytic distillation hydrodesulfurization device are re-reacted through the MTBE re-reaction device to obtain high-yield MTBE;
The catalytic distillation hydrodesulfurization device comprises an etherification reactor, a first distillation tower, a second distillation tower, a catalytic distillation tower, a first condenser, a stripping tower, an alkaline washing tank, a gate valve, a reflux pump, a second condenser, an extraction tower and a methanol tower, wherein an outlet of the etherification reactor is connected with an inlet of the first distillation tower, an outlet of the bottom of the first distillation tower is connected with an inlet of the second distillation tower, an outlet of the bottom of the second distillation tower is connected with an inlet in the middle of the catalytic distillation tower, a hydrogen inlet is further arranged at the lower part of the catalytic distillation tower, an outlet of the top of the second distillation tower is connected with an inlet of the first condenser, an outlet of the first condenser is connected with an inlet of the stripping tower, an outlet of the top of the stripping tower is connected with an inlet of the alkaline washing tank, a gate valve is arranged on a discharge pipeline at an outlet of the bottom of the stripping tower, an inlet of the reflux pump is communicated with, the outlet of the reflux pump is connected with a reflux port at the middle upper part of the catalytic distillation tower, the outlet at the bottom of the catalytic distillation tower is connected with the inlet of the second condenser, the outlet at the top of the first distillation tower is connected with the inlet of the extraction tower, and the outlet at the bottom of the extraction tower is connected with the inlet of the methanol tower;
The MTBE re-reaction device comprises an MTBE re-catalytic distillation tower, a methanol feed pump, a reboiler, a product pump, an MTBE finished product tank and a gas separation device header pipe, a first feed port in the side wall of the MTBE re-catalytic distillation tower is connected with a discharge port in the top of the extraction tower so as to enable unreacted C4 in the extraction tower to enter the MTBE re-catalytic distillation tower, a feed port of the methanol feed pump is communicated with a methanol outlet of the methanol tower, and a discharge port of the methanol feed pump is communicated with a methanol inlet of the MTBE catalytic distillation tower so as to enable methanol in the methanol tower to enter the MTBE catalytic distillation tower and react with C4 to generate MTBE continuously; the first discharge gate of MTBE re-catalytic distillation tower bottom is connected with the feed inlet of reboiler bottom to let the liquid phase thing of bottom in the tower naturally flow into the reboiler through gravity, the discharge gate and the MTBE re-catalytic distillation tower on the near lateral wall of bottom of reboiler top are connected, so that let the fluid after the heating get into the MTBE re-catalytic distillation tower, the second discharge gate and the feed inlet of product pump of MTBE re-catalytic distillation tower bottom are connected, so that go into the fluid pump of bottom in the tower product pump, the discharge gate of product pump is connected with the feed inlet of MTBE finished product jar, so that go into the fluid pump of bottom in the tower MTBE finished product jar, the gas outlet of gas-devided main pipe is connected with the bottom of MTBE re-catalytic distillation tower, lets in nitrogen gas, low pressure steam to the MTBE re-catalytic distillation tower.
2. The high yield MTBE catalytic distillation unit of claim 1, wherein: the MTBE re-reaction device also comprises an underground sump oil tank, wherein a feed inlet of the underground sump oil tank is connected with the bottom of the MTBE re-catalytic distillation tower so that sump oil enters the underground sump oil tank.
3. The high yield MTBE catalytic distillation unit of claim 1, wherein: the MTBE re-catalytic distillation tower includes stripping section, reaction section, rectification section, the stripping section is located the tower lower part, be equipped with the float valve tray in the stripping section, the reaction section is located the tower middle part, the reaction section is equipped with several sections reaction bed layers, all is provided with cyclic annular grid on every reaction bed layer, be equipped with the acidic ion exchange resin catalyst of bale formula hydrogen type in the cyclic annular grid, the rectification section is located tower upper portion, be equipped with regular packing and float valve tray in the rectification section.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920187946.1U CN209797875U (en) | 2019-02-02 | 2019-02-02 | High-yield MTBE catalytic distillation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920187946.1U CN209797875U (en) | 2019-02-02 | 2019-02-02 | High-yield MTBE catalytic distillation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209797875U true CN209797875U (en) | 2019-12-17 |
Family
ID=68821989
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920187946.1U Active CN209797875U (en) | 2019-02-02 | 2019-02-02 | High-yield MTBE catalytic distillation device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN209797875U (en) |
-
2019
- 2019-02-02 CN CN201920187946.1U patent/CN209797875U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP4174540B2 (en) | Industrial separation method of by-product alcohols | |
| CN112705124B (en) | Reactor, system for synthesizing carbonic ester and method for synthesizing carbonic ester | |
| JP4174541B2 (en) | Industrial separation of by-product alcohols | |
| CN105061165B (en) | Reaction apparatus for preparing polyoxymethylene dimethyl ether | |
| CN112299979B (en) | Method for extracting isobutyraldehyde | |
| US7470825B2 (en) | Reactor and process for producing methanol | |
| CN100395226C (en) | Method for mass producing butyl acetate by reactive distillation method and using sulfuric acid as catalyst | |
| CN209797875U (en) | High-yield MTBE catalytic distillation device | |
| CN201543256U (en) | Camphene distillation device | |
| US7287745B2 (en) | Liquid-continuous column distillation | |
| CN103214009B (en) | Synthesis ammonia decarburization technology | |
| CN102304048A (en) | Method and equipment for refining high-purity diethyl carbonate | |
| CN105622366B (en) | A kind of device and method for producing polymethoxy dimethyl ether DMM3 5 | |
| CN201762266U (en) | Trichloroethylene industrialized production device | |
| CN109232202B (en) | One-step method for synthesizing DMM 3-8 Apparatus and method of (2) | |
| CN208182895U (en) | A kind of tetrahydrofuran fractional order reaction separator | |
| CN100582071C (en) | Process and apparatus for catalytic distillations | |
| CN210261603U (en) | N-methyldiethanolamine production device | |
| CN214193101U (en) | Methyl mercaptan purification device | |
| CN208814917U (en) | A kind of formaldehyde reacts the catalytic rectifying tower for producing dimethoxym ethane with methanol | |
| CN208031945U (en) | A kind of catalytic distillation module applied to etherification reaction | |
| CN217612992U (en) | Mixed butyraldehyde separation and purification device | |
| CN112552217A (en) | Methyl mercaptan purification device | |
| CN1108844C (en) | Fractionating reaction column plate type catalytic distillating equipment | |
| CN209722049U (en) | Steady cracking formula gasoline catalyzing distills hydrodesulfurization unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |