CN204247174U - A kind of shell and tube reactor producing ethene and dimethyl ether - Google Patents
A kind of shell and tube reactor producing ethene and dimethyl ether Download PDFInfo
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- CN204247174U CN204247174U CN201420595963.6U CN201420595963U CN204247174U CN 204247174 U CN204247174 U CN 204247174U CN 201420595963 U CN201420595963 U CN 201420595963U CN 204247174 U CN204247174 U CN 204247174U
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Abstract
The utility model discloses a kind of shell and tube reactor producing ethene and dimethyl ether, the bottom of shell and tube reactor is provided with underfeed mouth, and underfeed mouth is connected with distribution gripper shoe, and distribution gripper shoe is connected with the tubulation of shell and tube reactor; The top of described shell and tube reactor is provided with reactant outlet, the top of shell and tube reactor is provided with upper feed inlet, connects distributor below upper feed inlet; A bottom reactant outlet is provided with in the bottom of shell and tube reactor.Great advantage of the present utility model is realized uniting two into one by the reactor of ethanol dehydration and methanol dehydration, take full advantage of the heating of methanol dehydration and the heat absorption feature of ethanol dehydration, solve methyl alcohol and ethanol mixed feeding is reacted, product dimethyl ether and ethylene separation and further Utilizing question.
Description
Technical field
The utility model belongs to petrochemical industry technique, particularly relates to a kind of petrochemical process process units.
Background technology
Ethene is the basic material of multiple important chemical products.Along with the development of World Economics, ethylene requirements amount grows with each passing day.Due to the rapid growth of China's economy, the annual growth of China's ethylene requirements amount exceedes world average level.The steam cracking being mainly derived from petroleum hydrocarbon raw material of ethene, crude oil price skyrockets in recent years, makes the production cost of cracking process ethene sharply increase.In addition, petroleum resources are as a kind of non-renewable resources, gradually exhausted, therefore develop the trend that renewable raw materials preparing ethylene becomes development.The bio-ethanol mainly renewable resource such as, stalk dry with corn, sugar, potato or lignocellulosic obtains through fermentation for raw material, and raw material sources are extensive, sufficient, can meet the needs of Large Scale Biology matter chemical industry development.China is a large agricultural country, and biomass resource enriches, and annual total output is not less than 1,000,000,000 tons of dries, if convert alcohol fuel to be equivalent to more than 300,000,000 ton of Petroleum Equivalent.Therefore be supplementing limited petroleum resources from ethanol preparing ethylene, also meet the strategy of sustainable development simultaneously.
Can be there is dehydration and generate ethene in ethanol, this technology realizes commercial Application after the twenties in 20th century under heating and catalytic condition.The ethanol dehydration catalyst having commercial Application to report at present is mainly divided into two large classes. i.e. activated alumina catalyst and molecular sieve catalyst.Nearest research finds, ethanol dehydration reaction has lower reaction temperature than aluminium oxide catalyst over a molecular sieve catalyst, higher operation air speed and the one way reaction conversion ratio of Geng Gao and yield of ethene.
From producing ethylene from dehydration of ethanol technique, generally adopt gas-phase dehydration method, because ethanol dehydration reaction caloric receptivity is larger, current reactor mainly adopts shell-and-tube reactor, the layered type reactor of catalyst bed interlayer heat exchange and insulation fix bed reactor, but this kind of reactor manufactures complexity, cost is higher, and catalyst loading and unloading is inconvenient.
US Patent No. 4134926 reports a kind of fluid bed that adopts to make the method for producing ethylene by ethanol dehydration, fluidized-bed reaction temperature controls at about 399 DEG C, ethanol conversion per pass is greater than 99.5%, and yield of ethene is greater than 99%, and catalyst uses active silica-alumina oxide.
Because ethanol dehydration reaction is a strong endothermic reaction, and its range of reaction temperature is narrower, and reaction temperature fluctuates the purity directly affecting product ethene, therefore provides heat to become particularly important to reaction system.From currently used process route, independent ethanol dehydration reaction technique is fixed bed, fluidized-bed reactor is all difficult to accomplish to maximize, and will directly have influence on economy and the competitive advantage of this technique like this.
Dimethyl ether is not only the intermediate of methanol synthesized gasoline, also be the important intermediate that synthesis gas produces hydro carbons simultaneously, a few days ago dimethyl ether alkene oneself obtain greater advance, particularly in catalyst, achieve comparatively quantum jump, primary study is carried out to dimethyl ether low-carbon alkene technique, petrochemicals will be produced for Non oil-based route and open up a Tiao Xin road.Therefore accelerate the development and utilization of dimethyl ether and high added value downstream product thereof, significant economic benefit and social benefit will be obtained.
Methanol dehydration generates in the reaction of dimethyl ether DME, by methanol gas phase dehydration method by methanol steam by solid catalyst generation heterogeneous catalytic reaction, conventional solid catalyst is activated alumina, crystalline aluminosilicate etc.The method be simple to operate, pollute little, quantity-produced new technology, its technical maturity, industrialization.Because Dehydration of methanol device is strong exothermal reaction, cold insufficient raw material, to reduce reaction bed temperature, therefore, under reaction temperature condition, is difficult to control bed temperature by the method.
Chinese patent CN200810000621 discloses the method that dimethyl ether is produced in the reaction of a kind of methanol oxidation distillation dehydration, adopts cationic ion-exchange resin to make catalyst, carries out the dehydration of methyl alcohol in catalytic distillation tower; The operating condition of catalytic distillation tower is: conversion zone middle portion temperature remains on 80 ~ 200 DEG C, tower top temperature is 10 ~ 110 DEG C, and bottom temperature is 130 ~ 260 DEG C, and operating pressure is 0.3 ~ 4.0MPa, overhead reflux ratio is 0.5 ~ 20, and feed volume air speed is 0.1 ~ 100 hour.But it controls reaction temperature by backflow heat-obtaining, and reaction heat is not well utilized.
Ethanol dehydration reaction is a strong endothermic reaction, and its range of reaction temperature is narrower, and reaction temperature fluctuates the purity directly affecting product ethene, therefore provides heat to become particularly important to reaction system.Meanwhile, Dehydration of methanol device is strong exothermal reaction, and cold insufficient raw material, to reduce reaction bed temperature, therefore, under reaction temperature condition, is difficult to control bed temperature by existing method.The energy that reaction produces well is utilized.The utility model is exactly both combinations reaction characteristics and proposes a kind of new composite reaction synthesizer.
Utility model content
Technical problem to be solved in the utility model is to provide the Association Technology Devices of a kind of producing ethylene from dehydration of ethanol and methanol dehydration dimethyl ether synthesis, thus can realize controlling bed temperature, and the energy that reaction is produced well is utilized.
In order to solve the problems of the technologies described above, the technical solution adopted in the utility model is:
A kind of shell and tube reactor producing ethene and dimethyl ether, comprise shell and tube reactor tank body, top end socket, bottom head, it is characterized in that: the bottom of described shell and tube reactor is provided with underfeed mouth, underfeed mouth is connected with distribution gripper shoe, and the top of described shell and tube reactor is provided with reactant outlet, the top of shell and tube reactor is provided with upper feed inlet, below upper feed inlet, connects distributor; A bottom reactant outlet is provided with in the bottom of shell and tube reactor.
A kind of shell and tube reactor producing ethene and dimethyl ether of the utility model, it is further characterized in that: described distribution gripper shoe is connected with in the tubulation pipe of shell and tube reactor; The now charging of upper feed inlet is entered by distributor between the pipe of shell and tube reactor.
A kind of shell and tube reactor producing ethene and dimethyl ether of the utility model, it is further characterized in that: be connected between described distribution gripper shoe with the tubulation pipe of shell and tube reactor; The now charging of upper port is entered in the pipe of shell and tube reactor by distributor.
A kind of shell and tube reactor producing ethene and dimethyl ether of the utility model, it is further characterized in that: described distribution gripper shoe has uniform pore openings, is porous distribution gripper shoe.After reaction raw materials enters from underfeed mouth through distribution gripper shoe be evenly distributed laggard enter shell-and-tube reactor pipe between or react in pipe.
A kind of shell and tube reactor producing ethene and dimethyl ether of the utility model, it is further characterized in that: between described distribution gripper shoe and low head, be provided with gripper shoe between pipe, for being supported on the catalyst loaded between tubular reaction organ pipe.
A kind of shell and tube reactor producing ethene and dimethyl ether of the utility model, it is further characterized in that: between described distribution gripper shoe, be provided with inlet ducts, distribute charging better.
A kind of shell and tube reactor producing ethene and dimethyl ether of the utility model, it is further characterized in that: described underfeed mouth is evenly provided with four.
A kind of shell and tube reactor producing ethene and dimethyl ether of the utility model, it is further characterized in that: described reactant outlet is evenly provided with four.
A kind of shell and tube reactor producing ethene and dimethyl ether of the utility model, it is further characterized in that: when described upper feed inlet enters ethanol raw material, underfeed mouth enters methanol feedstock.Conversely, when upper feed inlet enters methanol feedstock, underfeed mouth enters ethanol raw material.
A kind of shell and tube reactor producing ethene and dimethyl ether of the utility model, its concrete reactive applications is: between described tubular reaction organ pipe, be filled with ethanol dehydration catalyst, ethanol raw material contacts with each other from top between the pipe entering the shell and tube reactor that ethanol dehydration catalyst is housed after upper feed inlet enters distributor and ethanol dehydration catalyst and reacts, reaction temperature is 220 ~ 350 DEG C, reaction pressure is 0.15 ~ 0.5MPa, and catalyst quality air speed is 0.5 ~ 6h
-1, product ethene and water and a small amount of unreacted ethanol export out reactor from the bottom reactant between pipe.Be filled with methanol dehydration catalyst described tubular reaction organ pipe is in-built, material benzenemethanol from the underfeed mouth of tubular reactor after porous distribution gripper shoe is evenly distributed, enter interior the contacting with each other with methanol dehydration catalyst of the pipe that methanol dehydration catalyst is housed to react, reaction temperature is 220 ~ 350 DEG C, reaction pressure is 0.15 ~ 0.5MPa, and catalyst quality air speed is 0.5 ~ 8h
-1, generation dimethyl ether and water export out reactor from four reactants from reactor top; Logistics and logistics reverse flow in pipe between pipe.
Conversely, also can enter methanol feedstock by upper feed inlet, underfeed mouth enters ethanol raw material.Adopt this feeding manner, be arranged on by methanol dehydration catalyst between pipe, ethanol dehydration catalyst is arranged in pipe.Product ethene and water and a small amount of unreacted ethanol export out reactor from top reactant; Product dimethyl ether and water export out reactor from from reactor bottom reactant; Logistics and logistics reverse flow in pipe between pipe.
By adopting a shell and tube reactor, ethanol dehydration catalyst is housed between the pipe of shell and tube reactor, catalysis ethanol dehydration produces ethene, reaction is the endothermic reaction, at tubular reaction organ pipe built with methanol dehydration synthesizing dimethyl ether catalyst, make producing dimethyl ether by dehydrating methanol, react for exothermic reaction, institute's liberated heat provides heat for ethanol dehydration reaction.By the suction heat release of two reactions, realize the heat balance of heat release and the endothermic reaction, make reaction maintain stationary temperature scope and carry out.
Great advantage of the present utility model is realized uniting two into one by the reactor of ethanol dehydration and methanol dehydration, takes full advantage of the heat release of methanol dehydration and the heat absorption feature of ethanol dehydration, is in these two reaction temperatures of reacting same scope just in time simultaneously; Two liang of reaction logistics reverse flows, improve heat exchange efficiency; Three respectively discharging can be very easy to the separation realizing the material such as ethene, dimethyl ether, solve methyl alcohol and ethanol mixed feeding is reacted, product dimethyl ether and ethylene separation and further Utilizing question.
Accompanying drawing explanation
Fig. 1 is the combinations produce apparatus structure schematic diagram of a kind of ethene of the utility model and dimethyl ether.
Reference numeral shown in figure: 1-low head; 2-underfeed mouth; 3-distributes gripper shoe; 4-pipe inner catalyst; 5-inlet ducts; Catalyst between 6-pipe; 7-reactor tank body; The reactant outlet of 8-top; 9-upper cover; 10-distributor; 11-upper feed inlet; Gripper shoe between 12-pipe; Reactant outlet bottom 13-.
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is described in further detail, and specific embodiment does not limit the utility model.
As shown in Figure 1, a kind of shell and tube reactor producing ethene and dimethyl ether of the utility model comprises: shell and tube reactor tank body 7, low head 1, upper cover 9; Ethanol dehydration catalyst is filled with between described tubular reaction organ pipe, ethanol raw material between the pipe entering the shell and tube reactor that ethanol dehydration catalyst is housed after upper feed inlet 11 enters distributor 10 between top and pipe catalyst 6 to contact with each other reaction, reaction temperature is 220 ~ 350 DEG C, reaction pressure is 0.15 ~ 0.5MPa, and catalyst quality air speed is 0.5 ~ 6h
-1, product ethene and water and a small amount of unreacted ethanol go out reactor from the bottom reactant outlet 13 between pipe.
Be filled with methanol dehydration catalyst described tubular reaction organ pipe is in-built, material benzenemethanol from the underfeed mouth 2 of tubular reactor after porous distribution gripper shoe 3 is evenly distributed, enter interior the contacting with each other with pipe inner catalyst 4 of the pipe that methanol dehydration catalyst is housed to react, reaction temperature is 220 ~ 350 DEG C, reaction pressure is 0.15 ~ 0.5MPa, and catalyst quality air speed is 0.5 ~ 8h
-1, generation dimethyl ether and water go out reactor from four reactants outlets 8 from reactor top.
Logistics and logistics reverse flow in pipe between pipe, it is less that this mainly considers that initial reaction stage inhales thermal discharge, can the suction heat release in balanced reaction later stage better.Product enters that respective cooling tower realizes ethene, dimethyl ether is separated with a small amount of unreacted raw material with the water of production respectively, goes to enter respective subsequent fine cut respectively afterwards and obtains qualified superior product from systematic position; The dimethyl ether that reaction generates and water also directly enter next stage reaction, produce in the reactor of low-carbon alkene be further converted to ethene, propylene as dimethyl ether.
Claims (6)
1. produce the shell and tube reactor of ethene and dimethyl ether for one kind, comprise shell and tube reactor tank body, top end socket, bottom head, it is characterized in that: the bottom of described shell and tube reactor is provided with underfeed mouth, underfeed mouth is connected with distribution gripper shoe, described distribution gripper shoe is connected with in the tubulation pipe of shell and tube reactor, the top of described shell and tube reactor is provided with reactant outlet, the top of shell and tube reactor is provided with upper feed inlet, distributor is connected below upper feed inlet, the charging of upper feed inlet enters between the pipe of shell and tube reactor by distributor, a bottom reactant outlet is provided with in the bottom of shell and tube reactor.
2. the shell and tube reactor of production ethene according to claim 1 and dimethyl ether, is characterized in that: described distribution gripper shoe has uniform pore openings, is porous distribution gripper shoe.
3. the shell and tube reactor of production ethene according to claim 1 and dimethyl ether, is characterized in that: between described distribution gripper shoe and low head, be provided with gripper shoe between pipe.
4. the shell and tube reactor of production ethene according to claim 1 and dimethyl ether, is characterized in that: between described distribution gripper shoe, be provided with inlet ducts.
5. the shell and tube reactor of production ethene according to claim 1 and dimethyl ether, is characterized in that: described underfeed mouth is evenly provided with four.
6. the shell and tube reactor of production ethene according to claim 1 and dimethyl ether, is characterized in that: described reactant outlet is evenly provided with four.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420595963.6U CN204247174U (en) | 2014-10-10 | 2014-10-10 | A kind of shell and tube reactor producing ethene and dimethyl ether |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420595963.6U CN204247174U (en) | 2014-10-10 | 2014-10-10 | A kind of shell and tube reactor producing ethene and dimethyl ether |
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| CN204247174U true CN204247174U (en) | 2015-04-08 |
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| CN201420595963.6U Active CN204247174U (en) | 2014-10-10 | 2014-10-10 | A kind of shell and tube reactor producing ethene and dimethyl ether |
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