Device for co-production of tert-butyl alcohol and MTBE
By sending the remaining carbon 4 of the decarbonized four towers to the etherification reactor of the MTBE device for further processing, the maximum processing load of the decarbonized four towers and MTBE device is optimized, and the problems of low raw material utilization and poor economic benefits are solved. , realize efficient utilization and flexible adjustment, saving land and cost.
Patent Information
- Application Number
- CN202420062006.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-01-10
- Publication Date
- 2024-12-27
- Estimated Expiration
- 2034-01-10
AI Technical Summary
The raw material utilization rate of existing tert-butanol and MTBE independent devices is low, resulting in poor economic benefits and the inability to flexibly adjust the production load according to market supply and demand.
Design a MTBE device for co-producing tert-butanol. By sending the remaining carbon 4 produced by the decarbonized four towers to the etherification reactor of the MTBE device for further processing, the maximum processing load of the decarbonized four towers and the MTBE device is optimized. , realize efficient utilization and flexible adjustment of carbon 4.
It improves the comprehensive utilization rate of isobutene, increases the production volume and economic benefits of MTBE, saves land use and land resources, and reduces production costs.
Smart Images
Figure CN222240198U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of chemical synthesis, and particularly relates to a device for co-producing MTBE with tert-butyl alcohol. Background Art
[0002] Tert-butyl alcohol is used as raw material for producing tert-butylamine, isobutylene and triisobutylaluminum in the organic chemical industry, as paint solvent in the coating industry, as solvent and preparation of artificial musk in the pharmaceutical industry, for manufacturing flotation agent in the mining industry, as raw material for manufacturing fragrance in the fragrance industry, and for determining molecular weight in analytical chemistry.
[0003] MTBE is a colorless, transparent, high-octane liquid. Its main use is to produce an ideal blending component for unleaded, high-octane, oxygenated gasoline. It is widely used as a gasoline additive throughout the world.
[0004] The main raw materials of tert-butyl alcohol and MTBE units are mixed C4 components. In the refining enterprise, the above two production units are basically built independently. The isobutylene conversion rate of the decarbonization tower is about 75-80%, and the remaining isobutylene exists in the remaining C4. The remaining C4 produced is difficult to be used for further processing after leaving the unit, resulting in a low isobutylene utilization rate of the entire project and unable to generate better economic benefits. The MTBE unit has a single product, and the economic benefits of the unit are greatly affected by the market price fluctuations of MTBE. The processing of tert-butyl alcohol and MTBE independent units does not have the ability to flexibly adjust according to market supply and demand. Utility Model Content
[0005] In view of this, the utility model aims to provide a device for co-producing MTBE with tert-butyl alcohol to solve the problem of low raw material utilization.
[0006] In order to achieve the above object, the technical solution of the utility model is implemented as follows:
[0007] A device for co-producing tert-butyl alcohol and MTBE, comprising a tert-butyl alcohol device and a MTBE device, wherein the tert-butyl alcohol device and the MTBE device are connected via a C4 circulation pipeline;
[0008] The tert-butyl alcohol device comprises a multi-stage hydration reaction assembly and a decarbonization four-tower; a first mixed carbon four pipeline is provided on one side of the multi-stage hydration reaction assembly, and the multi-stage hydration reaction assembly is connected to the decarbonization four-tower through the pipeline.
[0009] The MTBE unit includes an etherification reactor, a catalytic distillation tower, and a methanol water washing recovery component;
[0010] The etherification reactor is connected to the catalytic distillation tower through a pipeline, and the catalytic distillation tower is connected to the methanol water washing recovery component through a pipeline; the methanol water washing recovery component is connected to the etherification reactor through a pipeline, the first mixed C4 pipeline is connected to the etherification reactor through the second mixed C4 pipeline, and an MTBE output pipeline is provided at the bottom of the catalytic distillation tower.
[0011] Furthermore, a desalted water pipeline is provided on the first mixed C4 pipeline, and a methanol pipeline is provided on the second mixed C4 pipeline.
[0012] Furthermore, the multi-stage hydration reaction assembly includes a primary hydration reactor, a secondary hydration reactor, and a tertiary hydration reactor;
[0013] The first mixed carbon four pipeline is connected to the upper part of the primary hydration reactor, the lower part of the primary hydration reactor is connected to the secondary hydration reactor through a pipeline, the bottom of the secondary water and reactor is connected to the tertiary hydration reactor through a pipeline, and the bottom of the tertiary water and reactor is connected to the middle part of the decarbonization four tower through a pipeline.
[0014] Furthermore, a tert-butanol outlet pipeline is provided at the bottom of the decarbonization tower, and a carbon four circulation pipeline and a second mixed carbon four pipeline are connected to the top of the decarbonization tower.
[0015] Further, the methanol water washing and recovery component includes a methanol water washing tower and a methanol recovery tower;
[0016] The top of the catalytic distillation tower is connected to the lower part of the methanol water washing tower through a pipeline, the bottom of the methanol water washing tower is connected to the methanol recovery tower through a circulating process water pipeline, and the bottom of the methanol recovery tower is connected to the upper part of the methanol water washing tower through a supplementary process water pipeline.
[0017] Furthermore, the top of the methanol recovery tower is connected to the second mixed C4 pipeline through a methanol recovery pipeline.
[0018] Furthermore, a post-ether C4 output pipe is provided on the top of the methanol water washing tower.
[0019] Compared with the prior art, the device for co-producing MTBE with tert-butyl alcohol described in the utility model has the following advantages:
[0020] 1. This application improves the utilization rate of isobutylene, an effective component in the raw material carbon four, and increases economic benefits by sending the remaining carbon four produced by the decarbonization four tower to the etherification reactor of the MTBE device for further processing. Taking a 50,000 tons / year decarbonization four tower and a 50,000 tons / year MTBE device as an example, the remaining carbon four is further processed through the etherification reaction process, and the comprehensive utilization rate of isobutylene is increased from 87% to more than 98%. Under the premise of the unchanged raw material processing volume, 15,000 tons / year of MTBE can be produced, and the economic benefits are increased by about 90 million yuan.
[0021] 2. This application optimizes the maximum processing load of the four decarbonization towers and the MTBE unit, and can flexibly adjust the processing load according to the market conditions of the two products.
[0022] Taking the 50,000 tons / year decarbonization tower and 50,000 tons / year MTBE unit as examples, the maximum processing load of the decarbonization tower is set to 91,000 tons / year, and the maximum processing load of MTBE is set to 109,000 tons / year. This can ensure that when any unit is shut down, the other unit can use up all the raw carbon four.
[0023] 3. This application sets up the decarbonization four-tower and MTBE device together through reasonable settings, saving industrial production land and reducing land resource waste. Taking the 50,000 tons / year decarbonization four-tower and 50,000 tons / year MTBE device as an example, the two devices are arranged independently, with a total area of about 10.5 acres, and the two devices are arranged together, with a total area of about 7.5 acres, reducing the land area by about 28% and reducing the land investment by about 2 million yuan. BRIEF DESCRIPTION OF THE DRAWINGS
[0024] The accompanying drawings constituting a part of the present invention are used to provide a further understanding of the present invention. The illustrative embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation on the present invention. In the accompanying drawings:
[0025] Figure 1 This is a schematic diagram of a device for co-producing MTBE from tert-butyl alcohol described in an embodiment of the utility model.
[0026] Description of reference numerals:
[0027] 1. Primary hydration reactor; 2. Secondary hydration reactor; 3. Tertiary hydration reactor; 4. Decarbonization tower 4; 5. Etherification reactor; 6. Catalytic distillation tower; 7. Methanol water washing tower; 8. Methanol recovery tower. DETAILED DESCRIPTION
[0028] It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments can be combined with each other.
[0029] The present invention will be described in detail below with reference to the accompanying drawings and in combination with embodiments.
[0030] like Figure 1As shown, a device for co-producing MTBE with tert-butyl alcohol includes a tert-butyl alcohol device and an MTBE device, wherein the tert-butyl alcohol device and the MTBE device are connected via a C4 circulation pipeline; the tert-butyl alcohol device includes a multi-stage hydration reaction component and a decarbonization tower 4; a first mixed C4 pipeline is provided on one side of the multi-stage hydration reaction component, and the multi-stage hydration reaction component is connected to the decarbonization tower 4 via a pipeline; the MTBE device includes an etherification reactor 5, a catalytic distillation tower 6, and a methanol water washing recovery component; the etherification reactor 5 is connected to the catalytic distillation tower 6 via a pipeline, and the catalytic distillation tower 6 is connected to the methanol water washing recovery component via a pipeline; the methanol water washing recovery component is connected to the etherification reactor 5 via a pipeline, the first mixed C4 pipeline is connected to the etherification reactor 5 via a second mixed C4 pipeline, and an MTBE output pipeline is provided at the bottom of the catalytic distillation tower 6. A desalted water pipeline is provided on the first mixed C4 pipeline, and a methanol pipeline is provided on the second mixed C4 pipeline.
[0031] The multi-stage hydration reaction assembly includes a primary hydration reactor 1, a secondary hydration reactor 2, and a tertiary hydration reactor 3; the first mixed carbon four pipeline is connected to the upper part of the primary hydration reactor 1, the lower part of the primary hydration reactor 1 is connected to the secondary hydration reactor 2 through a pipeline, the bottom of the secondary water and reactor is connected to the tertiary hydration reactor 3 through a pipeline, and the bottom of the tertiary water and reactor is connected to the middle part of the decarbonization four tower 4 through a pipeline.
[0032] The bottom of the decarbonization tower 4 is provided with a tert-butyl alcohol outlet pipeline, and the top of the decarbonization tower 4 is connected to the second mixed carbon four pipeline through a carbon four circulation pipeline. The methanol water washing recovery component includes a methanol water washing tower 7 and a methanol recovery tower 8; the top of the catalytic distillation tower 6 is connected to the lower part of the methanol water washing tower 7 through a pipeline, the bottom of the methanol water washing tower 7 is connected to the methanol recovery tower 8 through a circulating process water pipeline, and the bottom of the methanol recovery tower 8 is connected to the upper part of the methanol water washing tower 7 through a supplementary process water pipeline. The top of the methanol recovery tower 8 is connected to the second mixed carbon four pipeline through a methanol recovery pipeline. The top of the methanol water washing tower 7 is provided with an ether post-carbon four output pipe.
[0033] Implementation case 1:
[0034] (1) Implementation process of Case 1:
[0035] The raw material mixed carbon four is mixed with desalted water and enters the primary hydration reactor 1, and then enters the secondary hydration reactor 2 and the tertiary hydration reactor 3 in sequence. The reaction product enters the decarbonization tower 4, and the tertiary butyl alcohol product is extracted from the bottom of the decarbonization tower 4, and the remaining carbon four is extracted from the top of the decarbonization tower 4. 100% of the remaining carbon four is directly transported to the etherification reactor 5 through a pipeline to undergo etherification reaction with methanol. The discharge of the etherification reactor 5 enters the catalytic distillation tower 6, and the remaining isobutylene further reacts with methanol. The MTBE product is extracted from the bottom of the catalytic distillation tower 6, and the carbon four component containing methanol is extracted from the top of the tower and enters the methanol washing tower 7. In the methanol washing tower 7, methanol is absorbed by process water, and methanol aqueous solution is extracted from the bottom of the methanol washing tower 7. The methanol aqueous solution enters the methanol recovery tower 8, and the recovered methanol is extracted from the top of the methanol recovery tower 8 and used as a raw material for the etherification reaction process. The process water extracted from the bottom of the methanol recovery tower 8 is sent to the top of the methanol washing tower 7, and the remaining carbon four is extracted from the top of the methanol washing tower 7 and sent out of the boundary area.
[0036] Taking the 50,000 tons / year tert-butyl alcohol unit and the 50,000 tons / year MTBE unit as examples, the remaining C4 is further processed through the etherification reaction process, and the comprehensive utilization rate of isobutylene increases from 87% to more than 98%. Under the premise of unchanged raw material processing volume, the production of MTBE can be increased by 15,000 tons / year, and the economic benefits can be increased by about 90 million yuan / year.
[0037] (2) Implementation process of Case 2:
[0038] The raw material mixed carbon four is mixed with desalted water and enters the primary hydration reactor 1, and then enters the secondary hydration reactor 2 and the tertiary hydration reactor 3 in sequence. The reaction product enters the decarbonization tower 4, and the tertiary butyl alcohol product is extracted from the bottom of the decarbonization tower 4. The remaining carbon four is extracted from the top of the decarbonization tower 4. 50% of the remaining carbon four is directly transported to the etherification reactor 5 through a pipeline to undergo etherification reaction with methanol. The discharge of the etherification reactor 5 enters the catalytic distillation tower 6, and the remaining isobutylene further reacts with methanol. The MTBE product is extracted from the bottom of the catalytic distillation tower 6, and the carbon four component containing methanol is extracted from the top of the tower and enters the methanol washing tower 7. In the methanol washing tower 7, methanol is absorbed by process water, and methanol aqueous solution is extracted from the bottom of the methanol washing tower 7. The methanol aqueous solution enters the methanol recovery tower 8, and the recovered methanol is extracted from the top of the methanol recovery tower 8 and used as a raw material for the etherification reaction process. The process water extracted from the bottom of the methanol recovery tower 8 is sent to the top of the methanol washing tower 7, and the remaining carbon four is extracted from the top of the methanol washing tower 7 and sent out of the boundary area.
[0039] The process of implementation case 2 is consistent with the process of implementation case 1, and only the amount of residual carbon four entering the etherification reactor 5 is changed.
[0040] Taking the 50,000 tons / year tert-butyl alcohol unit and the 50,000 tons / year MTBE unit as examples, the remaining C4 is further processed through the etherification reaction step, and the comprehensive utilization rate of isobutylene increases from 87% to 93%. Under the premise of unchanged raw material processing volume, the production of MTBE can be increased by 9,000 tons / year, and the economic benefits can be increased by about RMB 54 million / year.
[0041] 2. Implementation Case 2:
[0042] (1) Implementation process of Case 3:
[0043] 100% of the raw material mixed with C4 is mixed with desalted water and enters the primary hydration reactor 1, and then enters the secondary hydration reactor 2 and the tertiary hydration reactor 3 in sequence. The reaction product enters the decarbonization tower 4, and the tertiary butyl alcohol product is extracted from the bottom of the decarbonization tower 4. The remaining C4 is extracted from the top of the decarbonization tower 4. The remaining C4 is directly transported to the etherification reactor 5 through a pipeline to undergo etherification reaction with methanol. The discharge of the etherification reactor 5 enters the catalytic distillation tower 6, and the remaining isobutylene further reacts with methanol. The MTBE product is extracted from the bottom of the catalytic distillation tower 6, and the C4 component containing methanol is extracted from the top of the tower and enters the methanol washing tower 7. In the methanol washing tower 7, methanol is absorbed by process water, and a methanol aqueous solution is extracted from the bottom of the methanol washing tower 7. The methanol aqueous solution enters the methanol recovery tower 8, and the recovered methanol is extracted from the top of the methanol recovery tower 8 and used as a raw material for the etherification reaction process. The process water extracted from the bottom of the methanol recovery tower 8 is sent to the top of the methanol washing tower 7, and the remaining C4 is extracted from the top of the methanol washing tower 7 and sent out of the boundary area.
[0044] Taking the 50,000 tons / year tert-butyl alcohol unit and the 50,000 tons / year MTBE unit as examples, the production load of the tert-butyl alcohol unit is 91,000 tons / year, and the production load of the MTBE unit is 15,000 tons / year.
[0045] (2) Implementation process of Case 4:
[0046] 50% of the raw material mixed C4 is mixed with desalted water and enters the primary hydration reactor 1, and then enters the secondary hydration reactor 2 and the tertiary hydration reactor 3 in sequence. The reaction product enters the decarbonization tower 4, and the tertiary butyl alcohol product is extracted from the bottom of the decarbonization tower 4. The remaining C4 is extracted from the top of the decarbonization tower 4. The remaining C4 is mixed with the remaining 50% of the raw material mixed C4 and then directly transported to the etherification reactor 5 through a pipeline for etherification reaction with methanol. The discharge of the etherification reactor 5 enters the catalytic distillation tower 6, and the remaining isobutylene further reacts with methanol. The MTBE product is extracted from the bottom of the catalytic distillation tower 6, and the C4 component containing methanol is extracted from the top of the tower and enters the methanol washing tower 7. In the methanol washing tower 7, methanol is absorbed by process water, and a methanol aqueous solution is extracted from the bottom of the methanol washing tower 7. The methanol aqueous solution enters the methanol recovery tower 8, and the recovered methanol is extracted from the top of the methanol recovery tower 8 and used as a raw material for the etherification reaction process. The process water extracted from the bottom of the methanol recovery tower 8 is sent to the top of the methanol washing tower 7, and the remaining C4 is extracted from the top of the methanol washing tower 7 and sent out of the boundary area.
[0047] The process of implementation case 4 is consistent with the process of implementation case 3, and only the amount of C4 mixed in the raw material entering the primary hydration reactor 1 is changed.
[0048] Taking the 50,000 tons / year tert-butanol unit and the 50,000 tons / year MTBE unit as examples, the production load of the tert-butanol unit is 50,000 tons / year, and the production load of the MTBE unit is 65,000 tons / year.
[0049] (3) Implementation process of Case 5:
[0050] 100% raw material mixed with C4 is transported to the etherification reactor 5, and undergoes etherification reaction with methanol. The discharge from the etherification reactor 5 enters the catalytic distillation tower 6, and the residual isobutylene further reacts with methanol. MTBE product is extracted from the bottom of the catalytic distillation tower 6, and the C4 component containing methanol is extracted from the top of the tower and enters the methanol water washing tower 7. In the methanol water washing tower 7, methanol is absorbed by process water, and methanol aqueous solution is extracted from the bottom of the methanol water washing tower 7. The methanol aqueous solution enters the methanol recovery tower 8, and methanol is extracted and recovered at the top of the methanol recovery tower 8 for use as a raw material for the etherification reaction step. The process water extracted from the bottom of the methanol recovery tower 8 is sent to the top of the methanol water washing tower 7, and the remaining C4 is extracted from the top of the methanol water washing tower 7 and sent out of the boundary area.
[0051] Compared with the implementation case 3, the tert-butyl alcohol unit of the implementation case 5 is shut down, and 100% of the raw material mixed with C4 directly enters the MTBE unit.
[0052] Taking the 50,000 tons / year tert-butanol unit and the 50,000 tons / year MTBE unit as examples, the production load of the tert-butanol unit is 0 tons / year, and the production load of the MTBE unit is 109,000 tons / year.
[0053] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.
Claims
1. A device for co-producing MTBE from tert-butyl alcohol, characterized in that: It includes a tert-butyl alcohol unit and an MTBE unit, and the tert-butyl alcohol unit and the MTBE unit are connected via a C4 circulation pipeline; The tert-butyl alcohol device comprises a multi-stage hydration reaction component and a decarbonization four-tower (4); a first mixed carbon four pipeline is provided on one side of the multi-stage hydration reaction component, and the multi-stage hydration reaction component is connected to the decarbonization four-tower (4) through the pipeline. The MTBE device comprises an etherification reactor (5), a catalytic distillation tower (6), and a methanol water washing recovery component; The etherification reactor (5) is connected to the catalytic distillation tower (6) through a pipeline, and the catalytic distillation tower (6) is connected to the methanol water washing recovery component through a pipeline; the methanol water washing recovery component is connected to the etherification reactor (5) through a pipeline, and the first mixed C4 pipeline is connected to the etherification reactor (5) through a second mixed C4 pipeline, and an MTBE output pipeline is provided at the bottom of the catalytic distillation tower (6).
2. A device for co-producing MTBE with tert-butyl alcohol according to claim 1, characterized in that: A desalted water pipeline is provided on the first mixed C4 pipeline, and a methanol pipeline is provided on the second mixed C4 pipeline.
3. A device for co-producing MTBE with tert-butyl alcohol according to claim 1, characterized in that: The multi-stage hydration reaction assembly comprises a primary hydration reactor (1), a secondary hydration reactor (2), and a tertiary hydration reactor (3); The first mixed carbon four pipeline is connected to the upper part of the primary hydration reactor (1), the lower part of the primary hydration reactor (1) is connected to the secondary hydration reactor (2) through a pipeline, the secondary water and the bottom of the reactor are connected to the tertiary hydration reactor (3) through a pipeline, and the tertiary water and the bottom of the reactor are connected to the middle part of the decarbonization four tower (4) through a pipeline.
4. A device for co-producing MTBE with tert-butyl alcohol according to claim 1, characterized in that: A tert-butyl alcohol outlet pipeline is provided at the bottom of the decarbonization tower (4), and the top of the decarbonization tower (4) is connected to the second mixed carbon four pipeline through a carbon four circulation pipeline.
5. The device for co-producing MTBE from tert-butyl alcohol according to claim 1, characterized in that: The methanol water washing and recovery component comprises a methanol water washing tower (7) and a methanol recovery tower (8); The top of the catalytic distillation tower (6) is connected to the lower part of the methanol water washing tower (7) through a pipeline, the bottom of the methanol water washing tower (7) is connected to the methanol recovery tower (8) through a circulating process water pipeline, and the bottom of the methanol recovery tower (8) is connected to the upper part of the methanol water washing tower (7) through a supplementary process water pipeline.
6. The device for co-producing MTBE from tert-butyl alcohol according to claim 5, characterized in that: The top of the methanol recovery tower (8) is connected to the second mixed C4 pipeline via a methanol recovery pipeline.
7. The device for co-producing MTBE from tert-butyl alcohol according to claim 5, characterized in that: The top of the methanol water washing tower (7) is provided with an ether post-C4 output pipe.