System and process for continuously producing butylene glycol and coproducing butanediol through butynediol hydrogenation

System and process for continuously producing butylene glycol and coproducing butanediol through butynediol hydrogenation

  • CN 106,397,129 B
  • Filed: 11/24/2016
  • Issued: 12/01/2020
  • Est. Priority Date: 11/24/2016
  • Status: Active Grant
First Claim
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1. A process for continuously producing butylene glycol and coproducing butylene glycol by hydrogenating butynediol is characterized by comprising the following steps:

  • 1) the method comprises the following steps that raw materials in a butynediol raw material tank (1) are uniformly mixed with desalted water and ammonia water through a mixer (3) through a butynediol raw material conveying pump (2), then the mixture is preheated through a decoloring preheater (4), the mixture enters a decoloring reactor (5) for reaction, and reaction liquid is sent into a decoloring filter (7) through a decoloring conveying pump (6), is decolored and purified, and then enters a to-be-reacted liquid metering tank (8);

    2) the solution to be reacted and hydrogen sent by a solution to be reacted metering pump (9) flow in parallel and enter a catalyst bed layer from the bottom of a first half hydrogenation reactor (10), the reaction heat is timely removed by the shell side water circulation of the first half hydrogenation reactor (10), the solution and the hydrogen react and then overflow to a first half hydrogenation gas-liquid separation tank (11), a part of separated hydrogen is pressurized by a recycle hydrogen compressor (13) and mixed with fresh hydrogen and then enters the first half hydrogenation reactor (10) again for cyclic utilization, the separated reaction solution is sent to a first crude butylene glycol metering tank (14) by a first half hydrogenation intermediate product conveying pump (12), the solution to be reacted and the hydrogen flow in parallel and enter the catalyst bed layer from the bottom of a second half hydrogenation reactor (16) by a first crude butylene glycol metering pump (15), and the reaction heat is timely removed by the shell side water circulation of the second half hydrogenation reactor (16), reacting with hydrogen, overflowing to a second half-hydrogenation liquid separation tank (18), mixing a part of separated hydrogen with fresh hydrogen by a recycled hydrogen compressor (13), and then re-entering a second half-hydrogenation reactor (16) for cyclic utilization, and conveying the separated reaction liquid to a second crude butylene glycol metering tank (20) by a second half-hydrogenation intermediate product conveying pump (19);

    3) the crude butanediol solution sent by the second crude butanediol metering pump (21) enters from the middle part of a butenediol lightness-removing tower (22), the gas phase at the top of the butenediol lightness-removing tower (22) enters a butenediol lightness-removing tower top condenser (23) after rectification, refining and separation, the gas phase at the top of the butenediol lightness-removing tower (22) enters a butenediol lightness-removing tower top reflux tank (24) after condensation, one part of the gas phase enters the upper part of the butenediol lightness-removing tower (22) to participate in reflux through a butenediol lightness-removing tower top reflux pump (25), the other part of the gas phase enters a butanediol full hydrogenation raw material tank (39), the liquid phase at the bottom of the butenediol lightness-removing tower (22) enters a butenediol heaving tower (27) from the middle part of the butenediol heaving tower (27) through a butenediol lightness-removing tower bottom conveying pump (26), the gas phase at the top of the butenediol heaving tower (27) enters a, then a part of the liquid phase at the bottom of the butenediol de-weighting tower (27) is sent to the upper part of the butenediol de-weighting tower (27) to participate in reflux, a part of the liquid phase at the bottom of the butenediol de-weighting tower (27) is sent to a butanediol total hydrogenation raw material tank (39) through a butenediol de-weighting tower bottom conveying pump (31), the solution sent to the butenediol product tower (32) enters from the middle part of the liquid phase, the gas phase at the top of the butenediol product tower (32) enters a butenediol product tower top condenser (33) after rectification, the gas phase at the top of the butenediol product tower (32) enters a butenediol product tower top reflux tank (34) after condensation, a part of the liquid phase at the bottom of the butenediol product tower (32) is sent to the upper part of the butenediol product tower (32) to participate in reflux through a butenediol product tower top reflux pump (35), a part of the liquid phase at the bottom of the butenediol product tower, the butenediol product extracted from the middle upper part of the butenediol product tower (32) enters a butenediol product intermediate extraction tank (36), and the butenediol product is obtained through a butenediol product intermediate extraction conveying pump (37);

    4) the solution to be reacted sent by the butanediol total hydrogenation metering pump (40) is preheated by the high-pressure total hydrogenation preheater (41), then flows with hydrogen in parallel to enter a catalyst bed layer from the top of the high-pressure total hydrogenation reactor (42), reacts with the hydrogen, is cooled by the high-pressure total hydrogenation cooler (43), then enters the total hydrogenation liquid separation tank (44), a part of the separated hydrogen is mixed with fresh hydrogen by the recovered hydrogen compressor (13), is pressurized by the high-pressure hydrogen machine compressor (17), then enters the high-pressure total hydrogenation reactor (42) again for recycling, and the separated reaction liquid is sent to the crude butanediol metering tank (46) by the high-pressure total hydrogenation intermediate product delivery pump (45);

    5) the crude butanediol solution sent by the crude butanediol metering pump (47) enters from the middle part of a butanediol lightness-removing tower (48), the gas phase at the top of the butanediol lightness-removing tower (48) enters a butanediol lightness-removing tower top condenser (49) after rectification, refining and separation, the gas phase at the top of the butanediol lightness-removing tower (48) enters a butanediol lightness-removing tower top reflux tank (50) after condensation, a part of the gas phase at the top of the butanediol lightness-removing tower (51) is sent to the upper part of the butanediol lightness-removing tower (48) to participate in reflux, a part of the gas phase at the top of the butanediol lightness-removing tower (48) is sent to a byproduct residue oil tank (65), the liquid phase at the bottom of the butanediol lightness-removing tower (48) is sent to a butanediol heaving tower (53) from the middle part of the butanediol heaving tower (53) through a butanediol lightness-removing tower bottom delivery pump (52), the gas phase at the top of the butanediol heaving tower (53) enters a butanediol heaving tower top condenser (54) after rectification, the butanediol heavi One part of the liquid phase at the bottom of the butanediol de-weighting tower (53) is sent to a byproduct residue oil tank (65) through a butanediol de-weighting tower bottom conveying pump (57), the solution sent to the butanediol product tower (58) enters from the middle part of the liquid phase, the gas phase at the top of the butanediol product tower (58) enters a butanediol product tower top condenser (59) after rectification, refining and separation, the gas phase enters a butanediol product tower top reflux tank (60) after condensation, one part of the liquid phase enters the upper part of the butanediol product tower (58) to participate in reflux through a butanediol product tower top reflux pump (61), one part of the liquid phase is sent to the byproduct residue oil tank (65), the liquid phase at the bottom of the butanediol product tower (58) is sent to the byproduct residue oil tank (65) through a butanediol product tower bottom conveying pump (64), the butanediol product extracted from the middle upper part of the butanediol product tower (58) enters a butanediol product middle extraction tank (62) of the butanediol product, a butanediol product is obtained by a butanediol product intermediate-extraction conveying pump (63);

    the butynediol raw material in the step

         1) is a mixed solution consisting of two or more of 1, 4-butynediol, water, propiolic alcohol, formaldehyde, methanol, formic acid, n-butyl alcohol and phenol.

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