CN214612313U - Device for recycling polluted methanol - Google Patents
Device for recycling polluted methanol Download PDFInfo
- Publication number
- CN214612313U CN214612313U CN202120605337.0U CN202120605337U CN214612313U CN 214612313 U CN214612313 U CN 214612313U CN 202120605337 U CN202120605337 U CN 202120605337U CN 214612313 U CN214612313 U CN 214612313U
- Authority
- CN
- China
- Prior art keywords
- inlet pipe
- methyl alcohol
- catalyst
- riser reactor
- 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
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a device of dirty methyl alcohol of resource recovery, belongs to methyl alcohol recovery plant technical field, including the riser reactor for carry out heavy oil catalytic cracking reaction, riser reactor bottom is provided with promotes gas inlet pipe and heavy oil inlet pipe in advance, it is provided with the methyl alcohol inlet pipe to promote the gas inlet pipe in advance, the methyl alcohol inlet pipe sets up atomizing component, atomizing component is used for atomizing dirty methyl alcohol. Dirty methyl alcohol becomes atomizing dirty methyl alcohol after getting into pre-lifting gas inlet pipe, and heavy oil gets into the riser reactor simultaneously, takes place the reaction in the riser reactor, and the device can turn into liquefied gas with 90% ~95% dirty methyl alcohol, has both improved the yield of liquefied gas in the catalytic cracking reaction, again with dirty methyl alcohol recycle, practices thrift the cost by a wide margin, has produced great economic benefits.
Description
Technical Field
The utility model belongs to the technical field of methyl alcohol recovery plant, concretely relates to device of dirty methyl alcohol of resource recovery.
Background
In the MTBE preparation process, methanol and isobutene are used as raw materials to produce MTBE, a large amount of polluted methanol containing impurities is generated, the polluted methanol passes through a methanol extraction tower firstly, impurities insoluble in water are removed, then the polluted methanol enters a methanol recovery tower, the polluted methanol discharged from the methanol recovery tower contains phenols, sulfur and other impurities, if the polluted methanol enters an MTBE device again, the catalyst can be poisoned, and if the polluted methanol is discharged, the great waste is caused, and the environment is polluted.
Disclosure of Invention
In view of the above, there is a need for a device for recycling contaminated methanol to solve the problems that contaminated methanol contains impurities such as phenols and sulfur, and if the contaminated methanol enters the MTBE device again, the catalyst is poisoned, and if the contaminated methanol is discharged, the waste is very large, and the environment is polluted.
An apparatus for resource recovery of contaminated methanol, the apparatus comprising: the riser reactor for carry out heavy oil catalytic cracking reaction, riser reactor bottom is provided with in advance and promotes gas inlet pipe and heavy oil inlet pipe, it is provided with the methyl alcohol inlet pipe to promote the gas inlet pipe in advance, the methyl alcohol inlet pipe sets up atomization component, atomization component is used for atomizing dirty methyl alcohol.
Preferably, the pre-lift gas feed pipe is further provided with a dry gas feed pipe and a vapour feed pipe, the methanol feed pipe being located above the dry gas feed pipe and the vapour feed pipe.
Preferably, the dry gas feed pipe is inclined and forms an acute angle with the steam feed pipe, and the steam feed pipe and the dry gas feed pipe are controlled by a proportional controller.
Preferably, the corner of pre-lifting gas inlet pipe is an arc-shaped corner, and the dry gas inlet pipe is arranged on the outer wall of the arc-shaped corner of the pre-lifting gas inlet pipe.
Preferably, the heavy oil inlet pipe, the methanol feeding pipe, the dry gas feeding pipe and the steam feeding pipe of the riser reactor are provided with flow control valves.
Preferably, the catalytic cracking device further comprises a settler, the settler is used for gas-solid separation and is provided with an oil mixture inlet, an oil gas outlet and a catalyst outlet, and the oil mixture inlet of the settler is connected with the oil mixture outlet of the riser reactor.
Preferably, the catalytic cracking apparatus further comprises a regenerator for catalyst regeneration, which is arranged at the lower part of the settler, a catalyst inlet of the regenerator is connected with a catalyst outlet of the settler, and a catalyst outlet of the regenerator is connected with a catalyst inlet of the riser reactor.
Preferably, a catalyst conveying pipe is arranged at the lower end of the regenerator, and a control valve is arranged on the catalyst conveying pipe.
The utility model adopts the above technical scheme, its beneficial effect lies in:
and (2) introducing the polluted methanol into a heavy oil catalytic cracking device, atomizing the polluted methanol, then introducing the polluted methanol into the riser reactor, introducing the heavy oil into the riser reactor, reacting in the riser reactor, and greatly increasing the content of liquefied gas in oil gas generated by the reaction. 90% -95% of the polluted methanol is converted into liquefied gas in the process, so that the waste and the environment pollution are avoided, the polluted methanol is recycled, the yield of the liquefied gas in the catalytic cracking reaction is improved, the polluted methanol is prevented from being used for the MTBE reaction to cause catalyst poisoning, the cost is greatly saved, and the great economic benefit is generated.
Drawings
FIG. 1 is a schematic structural diagram of a device for resource recovery of contaminated methanol.
In the figure: riser reactor 100, settler 200, regenerator 300, pre-lift gas feed line 110, catalyst transfer line 310, methanol feed line 111, dry gas feed line 112, vapor feed line 113.
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.
Please refer to fig. 1, which is a device for recycling contaminated methanol, and includes a riser reactor 100 for heavy oil catalytic cracking reaction, a pre-lift gas feeding pipe 110 and a heavy oil inlet pipe are disposed at the bottom of the riser reactor 100, the pre-lift gas feeding pipe 110 is provided with a methanol feeding pipe 111, the methanol feeding pipe 111 is an atomizing component, and the atomizing component is used for atomizing methanol.
Dirty methanol enters the pre-lift gas inlet pipe 110 from the methanol inlet pipe 111 to form atomized dirty methanol, the atomized dirty methanol enters the riser reactor 100 under the driving of the pre-lift gas, meanwhile, heavy oil enters the riser reactor 100 from the heavy oil inlet pipe to react, the content of liquefied gas in the generated oil gas is greatly increased, the dirty methanol is converted into liquefied gas in the process, the cost is reduced, and the economic benefit is improved.
Further, the pre-lift gas feed line is further provided with a dry gas feed line and a vapor feed line, and methanol feed line 111 is positioned above dry gas feed line 112 and vapor feed line 113.
Further, the dry gas feed pipe 112 is disposed obliquely and forms an acute angle with the vapor feed pipe 113, and the vapor feed pipe 113 and the dry gas feed pipe 112 are controlled by a proportional controller which can control the feed ratio of the dry gas and the vapor.
Further, the corners of pre-lift gas feed line 110 are curved corners and dry gas feed line 112 is disposed on the outer walls of the curved corners of pre-lift gas feed line 110 to facilitate drawing dry gas into pre-lift gas feed line 110 as vapor flows through the curved corners.
Further, the heavy oil inlet pipe, the methanol feed pipe 111, the dry gas feed pipe 112 and the vapor feed pipe 113 of the riser reactor 100 are provided with flow control valves, so that the feeding amount can be controlled conveniently.
Further, the catalytic cracking apparatus further comprises a settler 200, wherein the settler 200 is used for gas-solid separation and is provided with an oil mixture inlet, an oil gas outlet and a catalyst outlet, and the oil mixture inlet of the settler 200 is connected with the oil mixture outlet of the riser reactor 100.
Further, the catalytic cracking apparatus further comprises a regenerator 300, wherein the regenerator 300 is used for catalyst regeneration and is arranged at the lower part of the settler 200, a catalyst inlet of the regenerator 300 is connected with a catalyst outlet of the settler 200, and a catalyst outlet of the regenerator 300 is connected with a catalyst inlet of the riser reactor 100.
Further, a catalyst transfer pipe 310 is provided at a lower end of the regenerator 300, and a control valve is provided on the catalyst transfer pipe 310 so as to control the amount of the catalyst introduced into the riser reactor 100.
The technical effects of the present invention will be described in further detail below by way of specific examples:
example 1
Introducing 1.5t/h of steam into a pre-lifting gas feeding pipe 110 as pre-lifting gas, washing a dirty methanol mixture from an MTBE device with water, feeding the dirty methanol mixture into a methanol recovery tower, feeding the dirty methanol in the methanol recovery tower into a methanol feeding pipe 111, wherein the introduction amount of the dirty methanol is 0.5t/h, feeding the dirty methanol into the pre-lifting gas feeding pipe 110, atomizing the dirty methanol, enabling the dirty methanol to flow upwards in a riser reactor 100, introducing 22.8t/h of heavy oil through a heavy oil inlet pipe at the lower part of the riser reactor 100, simultaneously feeding a catalyst into the riser reactor 100 from an outlet of a regenerator 200, enabling the dirty methanol and the heavy oil to flow upwards under the driving of the pre-lifting gas, reacting in the riser reactor 100, wherein the reaction temperature is 520-620 ℃, and the reaction pressure is 0.1 MPa.
The generated oil mixture enters the settler 200 to realize gas-solid separation, the catalyst flows out from the catalyst outlet of the settler 200 and enters the regenerator 300 to be regenerated, and the regenerated catalyst flows out from the outlet of the regenerator 300 and enters the riser reactor 100 again to realize the reutilization of the catalyst. The oil gas flows out from the oil gas outlet of the settler 200, and gasoline, diesel oil, liquefied gas, dry gas and the like are obtained after post-treatment.
In order to verify the effect of the utility model, adopt the device and the process flow as shown in figure 1, the average value that the product distributes is obtained in a plurality of tests and is compared with the average value that the product distributes in the comparative example and can see table 1, wherein the comparative example is obstructed dirty methyl alcohol, and other conditions are all the same with example 1.
TABLE 1 product distribution
As can be seen from Table 1, compared with the experimental results of methanol without pollution, the yield of liquefied gas in the product obtained by the method of the utility model is increased by 1.9%, the yield of liquefied gas is increased by 0.456t in 24 hours on average, and the economic benefit is increased by 1459 yuan.
Example 2
Introducing 1.5t/h of steam into a pre-lifting gas feed pipe 110 to serve as pre-lifting gas, washing a dirty methanol mixture from an MTBE device, introducing the dirty methanol mixture into a methanol recovery tower, introducing the dirty methanol into a methanol feed pipe 111, wherein the introduction amount of the dirty methanol is 1t/h, introducing the dirty methanol into the pre-lifting gas feed pipe 110, atomizing the dirty methanol, enabling the dirty methanol to flow upwards in a riser reactor 100, introducing 22.8t/h of heavy oil through a heavy oil inlet pipe at the lower part of the riser reactor 100, introducing a catalyst into the riser reactor 100 from an outlet of a regenerator 200, enabling the catalyst to flow upwards by the pre-lifting gas to contact the dirty methanol and the heavy oil, reacting in the riser reactor 100, wherein the reaction temperature is 520-620 ℃, and the reaction pressure is 0.1 MPa.
The generated oil mixture enters the settler 200 to realize gas-solid separation, the catalyst flows out from the catalyst outlet of the settler 200 and enters the regenerator 300 to be regenerated, and the regenerated catalyst flows out from the outlet of the regenerator 300 and enters the riser reactor 100 again to realize the reutilization of the catalyst. The oil gas flows out from the oil gas outlet of the settler 200, and gasoline, diesel oil, liquefied gas, dry gas and the like are obtained after post-treatment.
In order to verify the effect of the present invention, the device and the process flow shown in fig. 1 are adopted, the average value of the product distribution obtained by a plurality of tests and the average value of the product distribution obtained by the comparative example are compared and shown in table 2, wherein the comparative example is the obstructed dirty methanol, and other conditions are the same as those of the embodiment 2.
TABLE 2 product distribution
As can be seen from Table 2, compared with the experimental result of methanol without pollution, the yield increase of the liquefied gas in the product obtained by the method of the utility model is 4.2%, the average 24-hour increase of the yield of the liquefied gas is 1.008t, and the economic benefit is increased by 3225 yuan.
Example 3
Introducing 1.5t/h of pre-lift gas into a pre-lift gas feed pipe 110, wherein the dry gas is 0.22 t/h, the steam is 1.28 t/h, a dirty methanol mixture from an MTBE device enters a methanol recovery tower through water washing, dirty methanol in the methanol recovery tower enters a methanol feed pipe 111, the introduction amount of the dirty methanol is 1t/h, the dirty methanol enters the pre-lift gas feed pipe 110, is atomized and flows upwards in a riser reactor 100, 22.8t/h of heavy oil is introduced through a heavy oil inlet pipe at the lower part of the riser reactor 100, meanwhile, a catalyst enters the riser reactor 100 from an outlet of a regenerator 200, is driven by the pre-lift gas to flow upwards to contact the dirty methanol and the heavy oil, and reacts in the riser reactor 100, the reaction temperature is 520-620 ℃, and the reaction pressure is 0.1 MPa.
The generated oil mixture enters the settler 200 to realize gas-solid separation, the catalyst flows out from the catalyst outlet of the settler 200 and enters the regenerator 300 to be regenerated, and the regenerated catalyst flows out from the outlet of the regenerator 300 and enters the riser reactor 100 again to realize the reutilization of the catalyst. The oil gas flows out from the oil gas outlet of the settler 200, and gasoline, diesel oil, liquefied gas, dry gas and the like are obtained after post-treatment.
To verify the effect of the present invention, the device and process flow as shown in fig. 1 were used, and the average value of the product distribution obtained by conducting a plurality of tests and the average value of the product distribution obtained by the comparative example were compared with each other, as shown in table 3, wherein the comparative example was steam as the pre-lift gas, and the other conditions were the same as those in example 3.
TABLE 3 product distribution
As can be seen from table 3, the comparison uses the steam as the experimental result of promoting the gas in advance, the utility model discloses a gasoline yield improves 0.54% in the product that the method obtained, and the diesel oil yield has improved 0.36%, and the liquefied gas yield has improved 0.1%, can practice thrift catalyst 270Kg on average every day, reduce cost 2700 yuan to the sewage discharge has been reduced.
Example 4
Introducing 1.5t/h of pre-lift gas into a pre-lift gas feed pipe 110, wherein the dry gas is 0.27t/h, the steam is 1.23t/h, a dirty methanol mixture from an MTBE device enters a methanol recovery tower through water washing, dirty methanol in the methanol recovery tower enters a methanol feed pipe 111, the introduction amount of the dirty methanol is 1t/h, the dirty methanol enters the pre-lift gas feed pipe 110, is atomized and flows upwards in a riser reactor 100, 22.8t/h of heavy oil is introduced through a heavy oil inlet pipe at the lower part of the riser reactor 100, meanwhile, a catalyst enters the riser reactor 100 from an outlet of a regenerator 200, is driven by the pre-lift gas to flow upwards to contact the dirty methanol and the heavy oil, and reacts in the riser reactor 100, the reaction temperature is 520-620 ℃, and the reaction pressure is 0.1 MPa.
The generated oil mixture enters the settler 200 to realize gas-solid separation, the catalyst flows out from the catalyst outlet of the settler 200 and enters the regenerator 300 to be regenerated, and the regenerated catalyst flows out from the outlet of the regenerator 300 and enters the riser reactor 100 again to realize the reutilization of the catalyst. The oil gas flows out from the oil gas outlet of the settler 200, and gasoline, diesel oil, liquefied gas, dry gas and the like are obtained after post-treatment.
To verify the effect of the present invention, the device and process flow as shown in fig. 1 were used, and the average value of the product distribution obtained by conducting a plurality of tests and the average value of the product distribution obtained by the comparative example were compared with each other, as shown in table 4, wherein the comparative example was steam as the pre-lift gas, and the other conditions were the same as those of example 4.
TABLE 4 product distribution
It can be seen from table 4 that the comparison uses the steam as the experimental result of promoting gas in advance, the utility model discloses a gasoline yield improves 0.6% in the product that the method obtained, and the diesel oil yield has improved 0.4%, and the liquefied gas yield has improved 0.1%, can practice thrift catalyst 289Kg on average every day, reduces cost 2890 yuan to sewage discharge has been reduced.
The device can also be filled with pure methanol to achieve the effect.
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 (8)
1. The utility model provides a device of dirty methyl alcohol of resource recovery which characterized in that, the device includes: the riser reactor for carry out heavy oil catalytic cracking reaction, riser reactor bottom is provided with in advance and promotes gas inlet pipe and heavy oil inlet pipe, it is provided with the methyl alcohol inlet pipe to promote the gas inlet pipe in advance, the methyl alcohol inlet pipe sets up atomization component, atomization component is used for atomizing dirty methyl alcohol.
2. The apparatus for resource recovery of contaminated methanol according to claim 1, wherein: the pre-lift gas feed pipe is further provided with a dry gas feed pipe and a vapor feed pipe, and the methanol feed pipe is located above the dry gas feed pipe and the vapor feed pipe.
3. The apparatus for resource recovery of contaminated methanol according to claim 2, wherein: the dry gas inlet pipe is obliquely arranged and forms an acute angle with the steam inlet pipe, and the steam inlet pipe and the dry gas inlet pipe are controlled by the proportional controller.
4. The apparatus for resource recovery of contaminated methanol according to claim 3, wherein: the corner of pre-lift gas inlet pipe is arc corner, the dry gas inlet pipe is arranged on the outer wall of the arc corner of the pre-lift gas inlet pipe.
5. The apparatus for resource recovery of contaminated methanol according to claim 1, wherein: and a heavy oil inlet, a methanol inlet pipe, a dry gas inlet pipe and a steam inlet pipe of the riser reactor are all provided with flow control valves.
6. The apparatus for resource recovery of contaminated methanol according to claim 1, wherein: the catalytic cracking device also comprises a settler, wherein the settler is used for gas-solid separation and is provided with an oil mixture inlet, an oil gas outlet and a catalyst outlet, and the oil mixture inlet of the settler is connected with the oil mixture outlet of the riser reactor.
7. The apparatus for resource recovery of contaminated methanol according to claim 6, wherein: the catalytic cracking device also comprises a regenerator, wherein the regenerator is used for regenerating a catalyst and is arranged at the lower part of the settler, a catalyst inlet of the regenerator is connected with a catalyst outlet of the settler, and a catalyst outlet of the regenerator is connected with a catalyst inlet of the riser reactor.
8. The apparatus for resource recovery of contaminated methanol according to claim 7, wherein: the lower end of the regenerator is provided with a catalyst conveying pipe, and the catalyst conveying pipe is provided with a control valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120605337.0U CN214612313U (en) | 2021-03-24 | 2021-03-24 | Device for recycling polluted methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120605337.0U CN214612313U (en) | 2021-03-24 | 2021-03-24 | Device for recycling polluted methanol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214612313U true CN214612313U (en) | 2021-11-05 |
Family
ID=78396950
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120605337.0U Active CN214612313U (en) | 2021-03-24 | 2021-03-24 | Device for recycling polluted methanol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214612313U (en) |
-
2021
- 2021-03-24 CN CN202120605337.0U patent/CN214612313U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106853957B (en) | Technology for preparing hydrogen peroxide by using palladium catalyst fixed bed anthraquinone method and alkali liquid separator thereof | |
| CN100579896C (en) | Method and system for preparing synthetic gas with appropriate hydrogen-carbon ratio from lurgi furnace outlet coal gas through non-catalytic partial oxidation by pure oxygen | |
| CN1137882C (en) | Full-circulating process for preparing urea | |
| CN214612313U (en) | Device for recycling polluted methanol | |
| CN111821821A (en) | Fusel oil recycling device and method in methanol production | |
| CN217163255U (en) | A rectification equipment that is arranged in N-methylaniline production methyl alcohol to retrieve | |
| CN102746904A (en) | Treating device and treating process for waste gas produced in pyrolysis of waste rubber and plastics | |
| CN210584487U (en) | Low-temperature methanol washing hydrogen sulfide treatment device | |
| CN210646336U (en) | Polyoxymethylene dimethyl ether synthesis and separation system | |
| CN203558989U (en) | Extraction system for polyoxymethylene dimethyl ether preparation device | |
| CN210796289U (en) | High-efficient low energy consumption sodium methoxide purification equipment | |
| CN210595940U (en) | Heat conduction oil processing device | |
| CN208038348U (en) | A kind of ammoxidation of propylene acrylonitrile production and Propylene Recovery System | |
| CN113058508A (en) | Device and method for recycling polluted methanol | |
| CN216273955U (en) | Heavy oil deep processing device | |
| CN216273956U (en) | High-efficiency heavy oil deep processing device | |
| CN206355622U (en) | A kind of PETROLEUM PROCESSING rectifying column | |
| CN204607890U (en) | A kind of device utilizing new catalytic rectifying structured packing to produce MTBE | |
| CN220736243U (en) | Device for reducing intermediate impurity content of extractant by extractant regeneration | |
| CN217448993U (en) | Organic mixed acid separation and purification device | |
| CN113121303B (en) | Chloroethylene production process and special device thereof | |
| CN215428945U (en) | Chloroethylene production device | |
| CN217119360U (en) | Rectification recovery device | |
| CN215667861U (en) | Light oil recovery device of hot potash decarburization system | |
| CN220968646U (en) | Device for purifying hydrogen sulfide and recycling excessive hydrogen |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: Device for recycling waste methanol Effective date of registration: 20220325 Granted publication date: 20211105 Pledgee: Ningxia East Guarantee Co.,Ltd. Pledgor: NINGXIA RUIKE CHEMICAL CO.,LTD. Registration number: Y2022640000004 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20230410 Granted publication date: 20211105 Pledgee: Ningxia East Guarantee Co.,Ltd. Pledgor: NINGXIA RUIKE CHEMICAL CO.,LTD. Registration number: Y2022640000004 |