CN102775274B - System and method for preparing ethylene glycol through oxalate hydrogenation - Google Patents
System and method for preparing ethylene glycol through oxalate hydrogenation Download PDFInfo
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- CN102775274B CN102775274B CN201110123872.3A CN201110123872A CN102775274B CN 102775274 B CN102775274 B CN 102775274B CN 201110123872 A CN201110123872 A CN 201110123872A CN 102775274 B CN102775274 B CN 102775274B
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Abstract
The invention discloses a system and a method for preparing ethylene glycol through oxalate hydrogenation. The system includes: a circulating hydrogen compressor, a charge and discharge heat exchanger, a heater, a mixer, a hydrogenation reactor, a raw material preheater, a reaction discharge cooler, and a gas-liquid separation tank. The method consists of: (a) heating a hydrogen charge material and an oxalate charge material respectively and then bringing them into the mixer, mixing them for complete gasification, and letting the gas enter the hydrogenation reactor directly; (b) subjecting a discharge material of the hydrogenation reactor to heat exchange with the hydrogen charge material and the oxalate charge material, cooling the discharge material and bringing it into the gas-liquid separation tank; and (c) making a liquid phase target product separated by the gas-liquid separation tank enter a subsequent separation unit, letting a hydrogen-rich gas phase enter systemic circulation, and maintaining a stable non-hydrogen gas content in the circulating hydrogen system through a discharge pipeline. Employment of the system and method disclosed in the inventive can effectively guarantee the needed reaction conditions, stably control the temperature rise of a reactor bed, full recover energy, reduce energy consumption, and ensure the conversion rate of oxalate and the selectivity of the ethylene glycol product.
Description
Technical field
The present invention relates to chemical field, say further, relate to a kind of system and method for hydrogenation of oxalate for preparing ethylene glycol.
Background technology
The ethylene glycol production method that petrochemical industry is traditional is that gaseous ethene and pure oxygen react and generate oxyethane, after oxyethane is separated from reaction discharging gas, then with water generation hydration reaction generating glycol.In traditional ethylene glycol production method, oxidation reactor and entry mixers manufacture and design difficulty, the interlocked control safe class of system requires high.Reason is that ethene directly mixes with pure oxygen, and strictly must control ethene within explosive range, and will avoid producing electrostatic, ethylene oxidation reactions is strong exothermal reaction simultaneously, easily temperature runaway occurs.Conventional aqueous reaction not only generates ethylene glycol in addition, and also have more Diethylene Glycol, triethylene glycol and many ethylene glycol to produce, the selectivity of ethylene glycol is about 90%.Need after hydration reaction to be separated to obtain ethylene glycol product through dehydration, purifying ethylene glycol link, cause that technical process is long, equipment is many, energy consumption is high, thus also directly have influence on the production cost of ethylene glycol.In recent years, oxyethane newly developed abroad and carbonic acid gas carry out esterification under catalyst action, then the ethylene carbonate ester process operational path of generating glycol is hydrolyzed, glycol selectivity is made to reach more than 99%, comparatively conventional aqueous has a clear superiority in, but this method still relies on oxyethane raw material.
Hydrogenation of oxalate for preparing ethylene glycol is an important directions of coal chemical industry, and its production method and technical process are in the research and development phase, there is no the barkite preparing ethylene glycol industrialized unit of a set of maturation at present in the world.The reaction more complicated of hydrogenation of oxalate for preparing ethylene glycol, under hydrogenation catalyst effect, hydrogenation reaction point multistep is carried out, and ethylene glycol is the intermediate product of reaction.
The main reaction occurred is as follows:
ROOCCOOR + 4H
2 → HOCH
2CH
2OH + 2ROH
The main side reaction occurred is:
HOCH
2CH
2OH + H
2 → CH
3CH
2OH + H
2O
Develop the system and method for rational hydrogenation of oxalate for preparing ethylene glycol, its object is just that reactive system can meet reaction requirement, and the transformation efficiency of reaction raw materials and the selectivity of ethylene glycol can ensure, simultaneity factor is arranged appropriately, take into full account energy-conservation.
The method of the preparing ethylene glycol from oxalic ester that Chinese patent CN101475442A announces uses two or more reactors in series, first barkite raw material, first strand of solvent and first strand of hydrogen enter the first reaction zone, contact with catalyst I, generate first strand of reaction effluent containing ethylene glycol; First strand of reaction effluent and second strand of solvent, second strand of hydrogen are mixed at least one second reaction zone, contact with catalyst I I, generate second strand of reaction effluent containing ethylene glycol.Aforesaid method object is the performance for ease of detecting catalyst, and in fact announcing in CN101475442A is more the feature of catalyzer, composition and the requirement to operational condition.
US Patent No. 4112245A discloses a kind of processing method of vapor phase process Hydrogenation ethylene glycol.The method includes the requirement to barkite raw material composition, temperature of reaction, reaction pressure, air speed, catalyzer and vector properties.US4112245A focuses on the impact emphasizing each factor, does not relate to technical process.
Summary of the invention
For solving problems of the prior art, the invention provides a kind of system and method for hydrogenation of oxalate for preparing ethylene glycol.Can the temperature rise of stability contorting reactor, efficient recovery energy, reduce energy consumption, ensure the transformation efficiency of barkite and the selectivity of product ethylene glycol.
An object of the present invention is to provide a kind of system of hydrogenation of oxalate for preparing ethylene glycol.
Comprise: circulating hydrogen compressor 1, input and output material interchanger 2, well heater 3, mixing tank 4, hydrogenator 5, feed preheater 6, reaction discharging water cooler 7 and knockout drum 8.
Input and output material interchanger 2 connects well heater 3 and mixing tank 4 successively, and feed preheater 6 connects mixing tank 4; Mixing tank 4 exports and connects hydrogenator 5 import, and hydrogen feed 9 enters hydrogenator 5 through input and output material interchanger 2, well heater 3 and mixing tank 4; Barkite charging 10 enters hydrogenator 5 through feed preheater 6 and mixing tank 4.
Hydrogenator 5 exports and connects input and output material interchanger 2, feed preheater 6, reaction discharging water cooler 7 and knockout drum 8 successively.
Knockout drum 8 top exit pipeline connects circulating hydrogen compressor 1 and input and output material interchanger 2 successively; Knockout drum 8 outlet at bottom is discharged outside liquid phase target product 11 to system.
Pipeline between knockout drum 8 and circulating hydrogen compressor 1 is provided with pipeline 12 of releasing.
Described mixing tank 4 is as far as possible near hydrogenator 5 entrance.
Described hydrogenator 5 is the combination of isothermal shell and tube reactor or isothermal shell-and-tube reactor and fixed bed adiabatic reactor.
Described well heater 3 is electrically heated, steam heating or process furnace.
Two of object of the present invention is to provide a kind of method of hydrogenation of oxalate for preparing ethylene glycol.
Comprise following steps:
A () hydrogen feed and barkite charging enter mixing tank mixing respectively after heating, barkite mixes with hydrogen and is gasified totally, and directly enter hydrogenator react with the form of gas phase.Hydrogenation reaction actuator temperature is 180 ~ 300 DEG C, and pressure is 2.0 ~ 6.0MPag, and weight space velocity is 0.01 ~ 10 h
-1;
The discharging of (b) hydrogenator successively with hydrogen feed and barkite charging heat exchange, through cooling after enter knockout drum;
C the isolated liquid phase target product of () knockout drum enters later separation unit, gas phase enters circulating hydrogen compressor, and it is stable to maintain non-hydrogen body burden in recycle hydrogen system by pipeline of releasing.
Specifically, method of the present invention can comprise hydrogenation reaction part, heat exchanger network part and recycle hydrogen part.
Hydrogenation reaction part comprises: raw hydrogen 9 mixes with recycle hydrogen, and through input and output material interchanger 2 preheating, then heater via 3 is heated to 150 ~ 350 DEG C of laggard mixing tanks 4.In mixing tank 4, hydrogen fully mixes with the barkite raw material 10 after preheating, and is vaporized completely by barkite.Mixed gas enters hydrogenator 5 with the temperature of 150 ~ 300 DEG C.Multilayer temperature point is set in hydrogenator, with detected temperatures distribution and maximum temperature rise.Be provided with high temperature interlocking in hydrogenator 5 entrance, outlet and bed, when temperature reaches set(ting)value, interlocking cuts off the thermal source of barkite charging 10 and well heater 3.
Heat exchanger network part comprises: hydrogenator 5 gas phase drop temperature is 180 ~ 350 DEG C.Reactor discharging and recycle hydrogen heat exchange, can be preheating to 110 ~ 250 DEG C by recycle hydrogen.Reaction discharging again with barkite raw material 10 heat exchange, barkite is preheating to 110 ~ 200 DEG C.Final reaction discharging is through being cooled to 40 ~ 100 DEG C of laggard knockout drums 8 further.
Recycle hydrogen part comprises: reaction discharging enters knockout drum 8 with the form of gas-liquid two-phase, and liquid phase target product 11 enters later separation unit, and gas phase removes circulating hydrogen compressor 1, compressor delivery pressure 2.0 ~ 6.0MPaG.Circulating hydrogen compressor 1 source line arranges pipeline 12 of releasing.Knockout drum arranges high level chain, when liquid level reaches interlocking liquid level, stops circulating hydrogen compressor, ensures the safety operation of unit.Containing impurity in hydrogen feed 9, in hydrogenator 5, side reaction produces by product, circulating hydrogen compressor source line arranges pipeline of releasing, discharges a small amount of gas by pipeline of releasing, avoid the accumulation of non-hydrogen gas in recycle hydrogen system, be beneficial to the stable operation of whole reactive system.Circulating hydrogen compressor can be reciprocating also can be centrifugal, and outlet line flow meter establishes low flow to interlock, and ensures recycle hydrogen flow, takes heat in hydrogenator in time out of.
Wherein:
Described hydrogen feed enters mixing tank after being heated to 150 ~ 350 DEG C.
Mixing tank is entered after described barkite charging is heated to 110 ~ 200 DEG C.
Described hydrogenator discharging enters knockout drum after being cooled to 40 ~ 100 DEG C.
Key of the present invention is that hydrogen feed heater via is heated to 150 ~ 350 DEG C of laggard mixing tanks, and barkite raw material mixes with hydrogen and vaporizes in mixing tank, directly enters hydrogenator with the form of gas phase.Both ensure that the vaporization requirement of reaction feed, and shortened again barkite as far as possible in the residence time of high-temperature zone, avoid decomposing.By the heating load of control heater, maintain the stable of hydrogenator temperature in.
Well heater form can be electrically heated, steam heating, also can be process furnace.
Hydrogenator service temperature is 180 ~ 300 DEG C, and working pressure is 2.0 ~ 6.0MPag, and weight space velocity is 0.01 ~ 10 h
-1lower reaction.
Oxalate hydrogenation is thermopositive reaction, for controlling the temperature rise of bed, type of reactor can adopt isothermal bed bioreactor, and reactor removes the mode of thermal recovery reactor shell-side generation steam or refrigerant cycle, multilayer temperature point is set waiting in hotbed, distributes with detected temperatures and control reaction temperature rising.When unit scale becomes large, the parallel operation of multiple stage isothermal bed bioreactor can be adopted; Or the mode adopting the hotbed parallel connections such as multiple stage to connect with adiabatic reactor again, to wait hotbed to control reaction temperature rising, ensure with adiabatic reactor the degree that reactant transforms.
Another key point of the present invention be reactor discharging first with recycle hydrogen heat exchange, and then with barkite charging heat exchange, cool finally by general facilities.This heat exchange order, both efficient recovery energy, turn avoid barkite and excessive temperature media for heat exchange and aggravate to decompose, being conducive to the yield that raising is reacted.
System and method tool of the present invention has the following advantages:
Adopt the type of reactor that isothermal reactor or isothermal reactor are connected with adiabatic reactor, both stability contorting reactor bed temperature rises, in turn ensure that abundant conversion.
Hydrogenator entrance arranges mixing tank, liquid phase barkite by with recycle hydrogen gas and vapor permeation after vaporize completely, directly enter hydrogenator with the form of gas phase, both met gas-phase feed requirement, at utmost shorten again raw material in the residence time of high-temperature zone, decrease the decomposition of barkite.
By rationally arranging heat exchange order, recovered energy to the full extent, reduce system energy consumption.It also avoid barkite and high-temperature medium heat exchange simultaneously, reduce the possibility of decomposing, improve reaction yield, ensure the transformation efficiency of barkite and the selectivity of ethylene glycol.
Accompanying drawing explanation
The reactive system schematic diagram of Fig. 1 embodiment 1 of the present invention
The reactive system schematic diagram of Fig. 2 embodiment 2 of the present invention
Description of reference numerals:
1---circulating hydrogen compressor 2---input and output material interchanger 3---well heater
4---mixing tank 5---hydrogenator 6---feed preheaters
7---reaction discharging water cooler 8---knockout drum 9---hydrogen feed
10---barkite charging 11---liquid phase target product 12---pipelines of releasing
13---cold medium.
Embodiment
Below in conjunction with embodiment, further illustrate the present invention, but the present invention is not by the restriction of embodiment.
embodiment 1
A system for hydrogenation of oxalate for preparing ethylene glycol, comprising: circulating hydrogen compressor 1, input and output material interchanger 2, well heater 3, mixing tank 4, hydrogenator 5, feed preheater 6, reaction discharging water cooler 7 and knockout drum 8.
Input and output material interchanger 2 connects well heater 3 and mixing tank 4 successively, and feed preheater 6 connects mixing tank 4; Mixing tank 4 exports and connects hydrogenator 5 import, and hydrogen feed 9 enters hydrogenator 5 through input and output material interchanger 2, well heater 3 and mixing tank 4; Barkite charging 10 enters hydrogenator 5 through feed preheater 6 and mixing tank 4.
Hydrogenator 5 exports and connects input and output material interchanger 2, feed preheater 6, reaction discharging water cooler 7 and knockout drum 8 successively.
Knockout drum 8 top exit pipeline connects circulating hydrogen compressor 1 and input and output material interchanger 2 successively; Knockout drum 8 outlet at bottom is discharged outside liquid phase target product 11 to system.
Pipeline between knockout drum 8 and circulating hydrogen compressor 1 is provided with pipeline 12 of releasing.
Hydrogenator 5 is single bed shell-and-tube reactor.
Well heater 3 is electric heaters.
Raw hydrogen 9 mixes with recycle hydrogen, reclaims after heat heated through input and output material interchanger 2, then heater via 3 be warming up to 250 DEG C after enter mixing tank 4.Raw material barkite 10 is preheated to 140 DEG C of laggard mixing tanks 4 through feed preheater 6.In mixing tank 4, hydrogen fully mixes with barkite, and is vaporized completely by barkite.
Hydrogenator 5 is entered in mixing tank 4 discharging, and for ensureing hydrogenation effect, hydrogenator 5 inlet operating temperature is at 200 ~ 250 DEG C, and working pressure is at 2.8 ~ 3.5MPaG.Weight space velocity is 0.1 ~ 1.0 h
-1.In hydrogenator 5, barkite and hydrogen reaction generating glycol.Hydrogenation reaction is thermopositive reaction, and a reaction heat part is removed thermal medium and taken away, and byproduct steam, another part heat goes out hydrogenator 5 with reflecting material strip.
Reaction discharging reclaims heat through heat exchanger network.First by input and output material interchanger 2 and recycle hydrogen heat exchange, laggard feed preheater 6 heating raw barkite 10.Reaction discharging, after feed preheater 6, is entered to react discharging water cooler 7, is entered knockout drum 8 after being cooled to 40 DEG C with the form of two phase flow.
The isolated liquid phase target product 11 of knockout drum 8 enters down-stream system.Density of hydrogen about 90mol% from the gas phase out of knockout drum 8 top, send circulating hydrogen compressor 1 as recycle hydrogen, the laggard recycle system of boosting.
Adopt barkite hydrogenation catalyst, catalyst weight air speed is 0.1 ~ 0.5 h
-1, bed maximum temperature rise 10 DEG C.
Adopt flow process as shown in Figure 1, obtain the result of table 1.
Result shows, adopt system and method preparing ethylene glycol of the present invention, isothermal reactor bed maximum temperature rise can control within 10 DEG C, the transformation efficiency of barkite is greater than 98%, glycol selectivity is greater than 90 mol%, by removing heat and heat exchanger network recovered energy, yield is 1.47Mkcal/t ethylene glycol.
Embodiment 2
System is identical with embodiment 1, and difference is only:
Hydrogenator 5 is that an isothermal shell-and-tube reactor is connected with an insulation fix bed reactor
Well heater 3 is steam heaters
Adopt barkite hydrogenation catalyst, catalyst weight air speed is 0.1 ~ 0.5 h
-1, bed maximum temperature rise is less than 10 DEG C.
Adopt flow process as shown in Figure 2, obtain the result of table 2.
Result shows, adopts system and method preparing ethylene glycol of the present invention, and isothermal reactor bed maximum temperature rise still can be controlled within 10 DEG C, waits hotbed barkite transformation efficiency to be greater than 85%.Unreacted barkite continues reaction at adiabatic reactor, and bed temperature rise is less than 5 DEG C.The overall conversion of barkite is greater than 98%, and ethylene glycol global selectivity is greater than 90 mol%, by removing heat and heat exchanger network recovered energy, and yield 1.45Mkcal/t ethylene glycol.
Claims (5)
1. the system of a hydrogenation of oxalate for preparing ethylene glycol, comprise: circulating hydrogen compressor (1), input and output material interchanger (2), well heater (3), mixing tank (4), hydrogenator (5), feed preheater (6), reaction discharging water cooler (7) and knockout drum (8), is characterized in that:
Input and output material interchanger (2) connects well heater (3) and mixing tank (4) successively, and feed preheater (6) connects mixing tank (4); Mixing tank (4) outlet connects hydrogenator (5) import, and hydrogen feed (9) enters hydrogenator (5) through input and output material interchanger (2), well heater (3) and mixing tank (4); Barkite charging (10) enters hydrogenator (5) through feed preheater (6) and mixing tank (4);
Hydrogenator (5) outlet connects input and output material interchanger (2), feed preheater (6), reaction discharging water cooler (7) and knockout drum (8) successively;
Knockout drum (8) top exit pipeline connects circulating hydrogen compressor (1) and input and output material interchanger (2) successively; Knockout drum (8) outlet at bottom discharges liquid phase target product (11) to outside system;
Pipeline between knockout drum (8) and circulating hydrogen compressor (1) is provided with pipeline of releasing (12);
Mixing tank (4) is near hydrogenator (5) entrance;
Described hydrogenator (5) is isothermal reactor, or isothermal reactor is connected with adiabatic reactor;
Described well heater (3) is electrically heated, steam heating or process furnace.
2. adopt a method for hydrogenation of oxalate for preparing ethylene glycol system as claimed in claim 1, it is characterized in that comprising following steps:
A () hydrogen feed and barkite charging enter mixing tank mixing respectively after heating, vaporize completely after barkite mixes with hydrogen, and directly enter hydrogenator reaction with the form of gas phase, hydrogenation reaction actuator temperature is 180 ~ 300 DEG C, pressure is 2.0 ~ 6.0MPag, and weight space velocity is 0.01 ~ 10h
-1;
The discharging of (b) hydrogenator successively with hydrogen feed and barkite charging heat exchange, through cooling after enter knockout drum;
C the isolated liquid phase target product of () knockout drum enters later separation unit, hydrogen rich gas at system internal recycle by circulating hydrogen compressor, and is maintained non-hydrogen body burden in recycle hydrogen system by pipeline of releasing and stablizes.
3. the method for hydrogenation of oxalate for preparing ethylene glycol as claimed in claim 2, is characterized in that: by arranging form that isothermal reactor or isothermal reactor connect with adiabatic reactor to control reaction temperature rising, and ensure transformation efficiency.
4. the method for hydrogenation of oxalate for preparing ethylene glycol as claimed in claim 2, it is characterized in that: hydrogenator (5) entrance arranges mixing tank (4), vaporize completely after liquid phase barkite and recycle hydrogen gas and vapor permeation, directly enter hydrogenator with gas phase.
5. method as claimed in claim 2, is characterized in that:
Described hydrogen feed enters mixing tank after being heated to 150 ~ 350 DEG C;
Mixing tank is entered after described barkite charging is heated to 110 ~ 200 DEG C;
Described hydrogenator discharging enters knockout drum after being cooled to 40 ~ 100 DEG C.
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| CN103467248B (en) * | 2013-09-02 | 2016-05-04 | 东华工程科技股份有限公司 | A kind of energy-saving ester through hydrogenation technique |
| CN104478658B (en) * | 2014-11-26 | 2017-05-03 | 西南化工研究设计院有限公司 | Technique and device for lowering hydrogen gas circulating rate in hydrogenation reaction process |
| CN104725191A (en) * | 2015-03-24 | 2015-06-24 | 中国五环工程有限公司 | Ethylene glycol refining and separating method and system |
| CN107082741B (en) * | 2017-06-16 | 2021-01-26 | 西南化工研究设计院有限公司 | Method for synthesizing ethylene glycol through oxalate deep hydrogenation catalytic reaction |
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| CN112759505B (en) * | 2019-10-21 | 2024-01-30 | 中国石油化工股份有限公司 | Method and system for preparing ethylene glycol |
| CN111018671B (en) * | 2020-01-03 | 2024-04-16 | 东华工程科技股份有限公司 | System for synthesizing ethylene glycol through dimethyl oxalate hydrogenation and preparation method thereof |
| CN111732497A (en) * | 2020-07-21 | 2020-10-02 | 濮阳永金化工有限公司 | Device for improving hydrogen-ester ratio and application method |
| CN115646377A (en) * | 2022-11-16 | 2023-01-31 | 陕西延长石油（集团）有限责任公司 | Reaction system and method for continuously producing alpha-alkyl ester |
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| JPS57122030A (en) * | 1981-01-22 | 1982-07-29 | Ube Ind Ltd | Continuous preparation of ethylene glycol |
| US4751334A (en) * | 1985-06-04 | 1988-06-14 | Davy Mckee (London) Limited | Process for the production of butane-1,4-diol |
| CN101462961A (en) * | 2008-01-28 | 2009-06-24 | 上海戊正工程技术有限公司 | Process flow for producing ethylene glycol with coproduction product dimethyl carbonate |
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2011
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4112245A (en) * | 1976-08-18 | 1978-09-05 | Atlantic Richfield Company | Process for the preparation of ethylene glycol |
| JPS57122030A (en) * | 1981-01-22 | 1982-07-29 | Ube Ind Ltd | Continuous preparation of ethylene glycol |
| US4751334A (en) * | 1985-06-04 | 1988-06-14 | Davy Mckee (London) Limited | Process for the production of butane-1,4-diol |
| CN101462961A (en) * | 2008-01-28 | 2009-06-24 | 上海戊正工程技术有限公司 | Process flow for producing ethylene glycol with coproduction product dimethyl carbonate |
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