CN-224207413-U - Preparation system of 1, 4-butanediol and co-production system of 1, 4-butanediol and alkyl-1, 4-butanediol

CN224207413UCN 224207413 UCN224207413 UCN 224207413UCN-224207413-U

Abstract

The utility model discloses a preparation system of 1, 4-butanediol and a co-production system of 1, 4-butanediol and alkyl-1, 4-butanediol. The 1, 4-butanediol preparation system uses a two-stage bubbling bed hydrogenation reactor, so that the service cycle of the catalyst can be effectively prolonged. Based on the system, the system for co-producing the alkyl-1, 4-butanediol can be obtained by arranging an aldehyde feeding end and a cocatalyst feeding end, so that the co-production of the 1, 4-butanediol and the alkyl-1, 4-butanediol is realized, and even the ratio of the alkyl-1, 4-butanediol in the product can be regulated and controlled to be up to 25wt%.

Inventors

LENG BINGWEN
ZHANG PEIDE
ZHANG XIAOMING
DENG ZHAOJING
WANG XIANFU
LIU BIN
BI YUNFEI
XIANG YONG
ZHAO FENG
LIANG WUYANG

Assignees

中化学科学技术研究有限公司
四川天华富邦化工有限责任公司

Dates

Publication Date: 20260508
Application Date: 20250528

Claims (10)

A system for preparing 1, 4-butanediol, the system comprising: a 1, 4-butynediol synthesis reactor; a formaldehyde recycle column downstream of the 1, 4-butynediol synthesis reactor; The first hydrogenation reactor and the second hydrogenation reactor are connected in series, and are bubbling bed hydrogenation reactors, and nickel-based catalyst layers are arranged in the first hydrogenation reactor and the second hydrogenation reactor; and a rectification unit downstream of the hydrogenation reactor.
2. The preparation system according to claim 1, wherein the 1, 4-butynediol synthesis reactor is provided with a feed inlet, a discharge outlet and a formaldehyde recycle inlet; The formaldehyde circulating tower is provided with a feed inlet and a discharge outlet; The discharge port of the 1, 4-butynediol synthesis reactor is connected with the feed port of the formaldehyde circulating tower, and the discharge port of the formaldehyde circulating tower is connected with the feed port or the formaldehyde circulating inlet of the 1, 4-butynediol synthesis reactor.
3. The preparation system according to claim 2, wherein the first hydrogenation reactor is provided with a feed inlet and a discharge outlet, and the discharge outlet of the formaldehyde recycling tower is connected with the feed inlet of the first hydrogenation reactor; The second hydrogenation reactor is provided with a feed inlet and a discharge outlet, the discharge outlet of the first hydrogenation reactor is connected with the feed inlet of the second hydrogenation reactor, and the discharge outlet of the second hydrogenation reactor is connected with the rectifying unit.
4. The production system of claim 3, wherein the feed inlet of the first hydrogenation reactor comprises a feed inlet for a reaction product of a1, 4-butynediol synthesis reactor and a hydrogen feed inlet; The feed inlet of the second hydrogenation reactor comprises a feed inlet of the first hydrogenation reactor product and a hydrogen feed inlet.
5. The production system according to claim 1, wherein the rectifying unit comprises a heavy removal column, a methanol recovery column downstream of the heavy removal column, and a light removal column downstream of the methanol recovery column.
6. The production system according to claim 5, wherein the de-heavies column, methanol recovery column and/or light ends column is a plate rectifying column.
7. The preparation system according to claim 5, wherein the heavy removal tower, the methanol recovery tower and the light removal tower are provided with a feed inlet, a gas phase discharge outlet and a liquid phase discharge outlet; The discharge port of the second hydrogenation reactor is connected with the feed port of the heavy-removal tower, the gas-phase discharge port of the heavy-removal tower is connected with the feed port of the methanol recovery tower, and the liquid-phase discharge port of the methanol recovery tower is connected with the feed port of the light-removal tower; Further, a liquid phase discharge port of the heavy component removing tower is used for extracting heavy components; The gas phase discharge port of the methanol recovery tower is used for extracting methanol and is connected with a device for preparing formaldehyde by oxidizing the methanol; The liquid phase discharge port of the light component removal tower is used for extracting 1, 4-butanediol, and the gas phase discharge port of the light component removal tower is used for extracting other alcohols except methanol.
A system for co-production of 8.1,4-butanediol and alkyl-1, 4-butanediol, characterized in that the system comprises the 1, 4-butanediol preparation system according to any one of claims 1-7, wherein the 1, 4-butanediol preparation system comprises or does not comprise a formaldehyde recycle column; The discharge port of the 1, 4-butynediol synthesis reactor is connected with the feed port of the first hydrogenation reactor; The system includes an aldehyde feed end for providing more aldehyde to the 1, 4-butenediol synthesis reactor and/or the first hydrogenation reactor; the first hydrogenation reactor and/or the second hydrogenation reactor are/is also provided with a cocatalyst feeding end.
9. The system of claim 8, wherein the aldehyde feed ends are disposed at a feed inlet of the 1, 4-butynediol synthesis reactor and/or at the top, upper, middle, and/or bottom of the first hydrogenation reactor.
A system for co-production of 10.1,4-butanediol and alkyl-1, 4-butanediol, the system comprising: a 1, 4-butynediol synthesis reactor; a formaldehyde recycle column downstream of the 1, 4-butynediol synthesis reactor; The first hydrogenation reactor and the second hydrogenation reactor are connected in series, the first hydrogenation reactor and the second hydrogenation reactor are bubbling bed hydrogenation reactors, nickel-based catalyst layers are arranged in the first hydrogenation reactor and the second hydrogenation reactor, and a cocatalyst feeding end is arranged in the first hydrogenation reactor and/or the second hydrogenation reactor; The aldehyde feeding end is used for providing more aldehyde for the 1, 4-butynediol synthesis reactor and/or the first hydrogenation reactor, and is arranged at the feed inlet of the 1, 4-butynediol synthesis reactor and/or at the top, upper part, middle part and/or bottom of the first hydrogenation reactor; And a rectification unit positioned at the downstream of the hydrogenation reactor, wherein the rectification unit comprises a heavy-removal tower, a methanol recovery tower positioned at the downstream of the heavy-removal tower and a light-removal tower positioned at the downstream of the methanol recovery tower.

Description

Preparation system of 1, 4-butanediol and co-production system of 1, 4-butanediol and alkyl-1, 4-butanediol Technical Field The utility model belongs to the field of chemical industry, and particularly relates to a preparation system of 1, 4-butanediol and a co-production system of 1, 4-butanediol and alkyl-1, 4-butanediol. Background 1, 4-Butanediol (BDO), which is commonly used for producing Tetrahydrofuran (THF), polytetrahydrofuran (PTMEG), gamma-butyrolactone (GBL), N-pyrrolidone and the like, is also commonly used for synthesizing degradable materials such as polyester PBS, PBAT, PBT and the like. Alkyl-1, 4-butandiol (MBDO), especially 2-methyl-1, 4-butandiol, has similar properties to BDO, and also downstream modified products of the same type as BDO, have other properties which are superior to BDO because the side chains contain methyl groups. For example, 3-methyltetrahydrofuran synthesized by MBDO can be used as a raw material in the pharmaceutical industry, can be polymerized with other monomers, can be used as a prepolymer in the industries of chemical fiber, TPU, slurry and the like, and greatly improves the low-temperature performance and the human body affinity of the elastomer. The polymer obtained by polymerization has better ductility and low temperature resistance because the side chains of the molecules contain methyl branched chains. Currently MBDO is mainly sourced as byproduct of BDO production equipment, particularly about 0.1-0.3% MBDO is generally byproduct of the Rappet BDO equipment, and is usually removed as impurity. For example, patent document CN 219232322U discloses a two-stage hydrogenation apparatus employing a stirred tank in series with a fixed bed, but the apparatus is used to suppress the BDO apparatus byproduct MBDO, and mentions that the conventional two-stage hydrogenation reactor is a trickle bed, the flow rate of the bed layer is slow, and the local high temperature affects the life of the catalyst. That is, based on the existing BDO device, no production device capable of directly synthesizing MBDO is available, and the BDO product with adjustable MBDO concentration is more difficult to obtain. Disclosure of Invention In order to improve the technical problems, the present invention provides a system for preparing 1, 4-butanediol, comprising: a 1, 4-butynediol synthesis reactor; a formaldehyde recycle column downstream of the 1, 4-butynediol synthesis reactor; The first hydrogenation reactor and the second hydrogenation reactor are connected in series, and are bubbling bed hydrogenation reactors, and nickel-based catalyst layers are arranged in the first hydrogenation reactor and the second hydrogenation reactor; and a rectification unit downstream of the hydrogenation reactor. According to an embodiment of the utility model, the 1, 4-butynediol synthesis reactor is provided with a feed port (such as a formaldehyde feed port, an acetylene feed port) and a discharge port, or is further provided with a formaldehyde recycle inlet; The formaldehyde circulating tower is provided with a feed inlet and a discharge outlet; The discharge port of the 1, 4-butynediol synthesis reactor is connected with the feed port of the formaldehyde circulating tower, and the discharge port of the formaldehyde circulating tower is connected with the feed port or the formaldehyde circulating inlet of the 1, 4-butynediol synthesis reactor. According to an embodiment of the utility model, the 1, 4-butynediol synthesis reactor is further provided with a tail gas outlet. According to an embodiment of the utility model, the first hydrogenation reactor is provided with a feed inlet and a discharge outlet, and the discharge outlet of the formaldehyde recycling tower is connected with the feed inlet of the first hydrogenation reactor. According to an embodiment of the utility model, the second hydrogenation reactor is provided with a feed inlet and a discharge outlet, the discharge outlet of the first hydrogenation reactor is connected with the feed inlet of the second hydrogenation reactor, and the discharge outlet of the second hydrogenation reactor is connected with the rectifying unit. According to an embodiment of the utility model, the feed inlet of the first hydrogenation reactor comprises a feed inlet for the reaction product of a1, 4-butynediol synthesis reactor and a hydrogen feed inlet. According to an embodiment of the utility model, the feed inlet of the second hydrogenation reactor comprises a feed inlet for the first hydrogenation reactor product and a hydrogen feed inlet. According to an embodiment of the utility model, the rectification unit comprises a heavy removal column, a methanol recovery column positioned downstream of the heavy removal column, and a light removal column positioned downstream of the methanol recovery column. According to an embodiment of the utility model, the de-heavies column, methanol recovery column and/or light ends column is a plate rectifying colum