CN206089502U - Reaction system of preparation ethylene of external heating - Google Patents

Abstract

The utility model relates to a reaction system of preparation ethylene of external heating. The system includes: thick liquid attitude bed reactor, condenser, condensation separator, liquor condensate storage tank, solvent pump, filtration equipment, green oil desorption system and solvent heater, thick liquid attitude bed reactor includes casing and sieve, the lower part of casing is equipped with reaction gas entry, solvent steam inlet, liquid outlet, the upper portion of casing is equipped with gas outlet and liquid inlet, the sieve is located the casing, fixes on shells inner wall, be located liquid inlet under, on reaction gas entry, the solvent steam inlet. The utility model discloses can effectively solve the problem that prior art preparation ethylene makeed inside heat be difficult for spreading, catalyst utilization efficiency is low.

Description

A kind of reaction system for preparing ethene of external heat

Technical field

The utility model generally relates to the preparation field of ethene, and in particular to a kind of reaction system for preparing ethene of external heat System.

Background technology

Ethene is a kind of important basic material in modern industry, is also one of maximum chemicals of world wide production, and it is produced Product are widely used in the fields such as national economy, people's lives, national defence, are " mothers of organic synthesis ".In the face of the shortage of petroleum resources Soaring with international oil price, raw material sources become the bottleneck of development ethylene industry, are also asking of must solving in face of people of pendulum Topic.Therefore, research and develop a kind of new technology to prepare ethene, to be allowed to petroleum replacing as industrial raw materials, can Alleviate dependence of the modern industry to oil.

In coal chemical technology, Non-catalytic partial is passed through by calcium carbide technique, or by raw material of natural gas by raw material of coal Oxidation technology produces acetylene, it has also become maturation process.Again with acetylene as raw material, in the presence of selective hydrocatalyst, lead to Cross hydrogenation process and obtain ethylene product, can further expand Coal Chemical Industry Route.Therefore, the new technology of producing ethylene with acetylene hydrogenation is developed Technology, has broad application prospects.

Low concentration acetylene gas and solid phase catalyzing hydrogen addition technology is highly developed in the oil industry, is mainly used in being removed in ethene Acetylene impurities, the reactor for using is fixed bed reactors, and solid-phase catalyst is loaded in the reactor carries out gas-solid phase reaction.But Because ethyne reactive is high, hydrogenation reaction thermal discharge is big, even there is a small amount of acetylene in cracking gas, traditional gas is solid phase fixed bed Hydrogenation reactor there are still the serious problems such as green oil generating amount is big, catalyst cycle period is short, reactor easy " temperature runaway ".

Prior art one is a kind of fluidized-bed process and device of producing ethylene with acetylene hydrogenation.The technique is comprised the following steps： Catalyst and diluent are added in fluidized-bed reactor；Heating reduction is carried out to catalyst；Acetylene and hydrogen mixture are led to Fluidized bed reactor；Selective hydrogenation of acetylene generates ethene；Cooling medium is passed through reactor heat exchange component to remove reaction Heat；Isolated ethylene product.The technology is suffered from the drawback that：

Preparing ethylene by selective hydrogenation of acetylene is strong exothermal reaction, although in the process cooling medium is to remove during reaction The substantial amounts of heat released, but still it is difficult to that gas temperature too high hidden danger in local when reacting is completely eliminated；

Because of the fluid bed that the technique is used, the mutual sharp impacts of catalyst particles intergranular are just difficult to avoid that, this can bring catalysis The problems such as abrasion of the loss of agent, the difficulty for increasing dedusting, increase heat exchange component and reactor.

Prior art two is continuously separated production line for a kind of ethene, including oxygen hydrogenation reactor, the drier of cracking gas second, Removal of mercaptans/cos reactor, dearsenification reactor, acetylene hydrogenation reactor.What its acetylene hydrogenation reactor for using was adopted Reactor is fixed bed reactors.It is merely able to process the acetylene of low concentration, and treating capacity is smaller；If acetylene content increases, A large amount of green oils can be generated, is caused catalyst cycle period to shorten, the problem of reactor " temperature runaway " is even occurred.

Therefore, in order that reactor adapts to larger amount of reaction acetylene gas, do not result in catalyst utilization it is low, The problem of reactor " temperature runaway ", removes in time green oil, fundamentally improves gas-liquid flow field distribution, improves the matter of fluidisation in reactor Amount, it is necessary to propose a kind of new reaction system for preparing ethene.

Utility model content

The purpose of this utility model is to provide a kind of reaction system for preparing ethene of external heat, to solve prior art Ethene is prepared so that internal heat is difficult to spread out of, green oil is more, the problem that catalyst utilization is low.

The utility model provides a kind of reaction system for preparing ethene of external heat, and it includes：Paste state bed reactor, condensation Device, condensation separator, condensate tank, solvent pump, filter plant, green oil removing system and solvent heater；Wherein described slurry State bed reactor includes housing and sieve plate；The bottom of the housing is provided with reaction gas inlet, solvent vapo(u)r entrance, liquid discharge Mouthful；The top of the housing is provided with gas vent and liquid inlet；The sieve plate is located in the housing, is fixed on the housing On inwall, under the liquid inlet, on the reaction gas inlet, the solvent vapo(u)r entrance；The solvent adds Hot device is connected by the solvent vapo(u)r entrance with the paste state bed reactor, and the bottom of towe solvent tank passes through the liquid discharge Mouth is connected with the paste state bed reactor, and the condenser is connected by the gas vent with the paste state bed reactor, institute State solvent pump to connect with the paste state bed reactor by the liquid inlet；It is the condenser, the condensation separator, described Condensate tank and the solvent pump are sequentially communicated；The filter plant is connected with the condensate tank；The filter plant, The green oil removing system and the solvent heater are sequentially communicated.

Above-mentioned system, in the condensate tank agitating device is provided with.

Above-mentioned system, the condensation separator connects ethene collection device.

Above-mentioned system, is dispersed with the sieve plate that multilayer is parallel to each other, the sieve plate of adjacent layer inside the paste state bed reactor Between it is spaced, the interval of each layer sieve plate is equal.

Above-mentioned system, per layer of sieve plate includes seal pot, bubbling area, downflow weir and downspout；Wherein, the sieve plate Part edge fix with the inner walls；The part that the part edge of the fixation fences up with the downflow weir is by liquid Disk；For holding the liquid flowed down from downspout described in upper strata；The centre of the seal pot is distributed with sieve aperture, forms bubbling Area, the bubbling area is the main region of gas liquid reaction；The downflow weir is located at revocable edge of the sieve plate, described to overflow Stream weir is higher than the seal pot of place layer, for keeping the height of liquid on per layer of sieve plate；The downspout is used to make liquid The seal pot of sieve plate described in lower floor is flow to from the downflow weir of sieve plate described in upper strata, positioned at the side of the downflow weir.

Above-mentioned system, the sieve aperture is equally distributed circular aperture, and the centre-to-centre spacing of the aperture is the 1-5 in aperture Times, a diameter of 5-20mm of the aperture.

Above-mentioned system, the sieve aperture of the sieve plate is provided with float valve or bubble-cap.

Above-mentioned system, the bottom of the downspout of sieve plate is not higher than the height of sieve plate downflow weir described in lower floor described in upper strata.

The beneficial effects of the utility model are, the utility model proposes a kind of new external heat prepares the anti-of ethene System and method is answered, the reaction system and method are simple to operation, course of reaction is easily achieved shifting heat, can remove in time green Oil, catalyst reusable edible so that carrying out high concentration selective hydrogenation of acetylene using paste state bed reactor becomes a kind of important Alkene processed production ways.

Description of the drawings

Fig. 1 prepares the structural representation of the paste state bed reactor of ethene for technical solutions of the utility model；

Fig. 2 is the overlooking the structure diagram of sieve plate in technical solutions of the utility model；And

Fig. 3 is the system architecture schematic flow sheet that technical solutions of the utility model embodiment prepares ethene.

Specific embodiment

Below in conjunction with drawings and Examples, specific embodiment of the present utility model is described in more details, with Just scheme of the present utility model and the advantage of its various aspects be better understood when.However, specific implementations described below Mode and embodiment are only descriptive purposes, rather than to restriction of the present utility model.

If Fig. 1 is the structure chart of the paste state bed reactor in the utility model.Wherein：1st, reaction gas inlet；2nd, liquid Outlet；3rd, gas vent；4th, liquid inlet；5th, sieve plate；6th, downspout；7th, solvent vapo(u)r entrance.

The principle of paste state bed reactor is gas in bubbling form by being suspended with liquid (slurries) layer of solid fine grain, with Realize the reactor of gas-liquid solid phase reaction process.This kind is used for the paste state bed reactor of preparing ethylene by selective hydrogenation of acetylene, described Paste state bed reactor includes reactor shell and sieve plate 5.

Reactor shell bottom is provided with reaction gas inlet 1, solvent vapo(u)r entrance 7 and liquid outlet 2, reactor shell Gas vent 3 is arranged at top.

The sieve plate 5 is located in the housing, is fixed in the inner walls, under the liquid inlet 4, institute State on reaction gas inlet 1, the solvent vapo(u)r entrance 7.

Middle part in reactor enclosure body, is evenly distributed sieve plate 5.Have on every layer of sieve plate 5 seal pot, downflow weir, Downspout 6 and bubbling area.Part edge and the inner walls of sieve plate are fixed, and revocable edge is provided with downflow weir.Fixed portion The part that point edge fences up with the downflow weir is seal pot, for holding the liquid flowed down from upper strata downspout.

The top view of sieve plate 5 is as shown in Figure 2.Being to maintain on every layer of sieve plate in the effect of the downflow weir of one end of sieve plate 5 has The liquid of certain altitude.Downspout 6 is next in downflow weir.Specifically, downspout can be by the downflow weir of the sieve plate and institute The gap for stating reactor wall is formed.Certainly it is such as pipeline configuration that downspout 6 may also be other structure.The effect of downspout 6 It is the seal pot for allowing liquid that lower floor's sieve plate is flow to from the downflow weir of upper strata sieve plate.The bottom of the downspout 6 of upper strata sieve plate 5 is not high In the height of the downflow weir of lower floor's sieve plate 5.So design is in order to realize fluid-tight, that is, to prevent gas from rising from downspout 6 and cause Each layer gas connects and short-circuit.Central region on sieve plate 5 is bubbling area, and circular aperture is uniform-distribution with thereon.Aperture is The main thoroughfare that gas rises, enables to gas and liquid uniform contact.

The downspout 6 of reactor adjacent layer is in being projected on circumferential angle on the direction of the seal pot It is staggeredly arranged.So conveniently realize that the liquid that upper strata sieve plate 5 flows down is stored in certain hour on adjacent lower sieve plate 5, until liquid Body is higher by the downflow weir of the lower floor and flows out to again the sieve plate 5 of lower floor.

Aperture can keep pitching row pattern state with the flow direction of liquid, and the arrangement mode of aperture can be positive trigonometric expression.Small hole center away from For 1-5 times of aperture, the centre-to-centre spacing between preferred hole is 1.5 times；A diameter of 5-20mm in hole, preferred hole it is a diameter of 10mm。

Float valve or bubble-cap can be also provided with the sieve aperture of sieve plate.Float valve can float on sieve plate, with gas flow Change and change its open degree.There is riser in bubble-cap, rotary space is formed between bubble-cap and riser.Riser is fixed on On sieve plate, gas phase enters rotary space by riser, is sprayed by slot with certain spouting velocity, with the liquid shape on sieve plate Into bubbling contact.

The reaction system for preparing ethene of external heat is illustrated in figure 3, it includes：The slurry bed system mentioned in described above is anti- Answer device 10, solvent heater 20, condenser 30, condensation separator 40, condensate tank 50, solvent pump 60, the and of filter plant 70 Green oil removes system 80.Solvent heater 20 is connected by the solvent vapo(u)r entrance with the paste state bed reactor 10, described Filter plant 70 is connected by the liquid outlet with the paste state bed reactor 10, and the condenser 30 is gone out by the gas Mouth is connected with the paste state bed reactor 10, and the solvent pump 60 is connected by the liquid inlet with the paste state bed reactor 10 It is logical；The condenser 30, the condensation separator 40, the condensate tank 50 and the solvent pump 60 are sequentially communicated；It is described Filter plant 70, green oil removing system 80 and the condensate tank 50 are sequentially communicated.

Above-mentioned system, in the condensate tank 50 agitating device is provided with, for solvent in condensate tank 50 with urge The stirring of agent.

Said system has solvent heater 20 in the outside of reactor, evaporates can liquid flux, there is provided continuous to rise Steam air-flow, while providing thermal source for whole reactor.

When preparing ethene, the gaseous mixture of acetylene and hydrogen is entered by the reaction gas inlet 1 of the bottom of paste state bed reactor 10 Enter in reactor.In the bottom solvent vapo(u)r entrance of reactor, steam to the lower and upper reactor that passes through, there is provided continuous to rise Steam air-flow, while providing thermal source for whole reactor.Reacting gas is as solvent vapo(u)r is together by the sieve of inside reactor Aperture on plate is entered among liquid phase.Wherein solvent vapo(u)r heats liquid flux by the solvent heater 20 outside reactor Evaporate and generate.Flow in the liquid inlet 4 on catalyst and carrier solvent autoreactor top.Because aperture is equal on sieve plate 5 Even distribution, so reacting gas is also evenly spread to therewith in the middle of liquid.In a liquid, reacting gas is in liquid is suspended in Catalyst catalytic action under react.Reacted gas departs from this layer of sieve plate 5, then by the aperture of upper strata sieve plate 5 Enter in the middle of supernatant liquid.So repeatedly up to by the sieve plate 5 of reactor the top, from the gas vent of reactor top 3 go out.

In the reactor, gas be to it is lower and on flow direction, liquid is flow direction from top to down, and gas phase and liquid phase are in integrally Reveal the direction of adverse current, increase the effect of mass transfer and heat transfer.Due to there is multiple sieve plate in reactor, that is, mean reaction Multiple little paste state bed reactors are there are in device, the contact area that gas-liquid-solid three-phase is fully contacted is increased, gas-liquid is improved Flow Field Distribution, it is to avoid short circuit, but also turbulence and gas-liquid mass transfer can be strengthened, improve the quality of fluidisation in reactor.

From reactor top reaction gas out, then gas temperature is cooled down by the cooling of condenser 30.Subsequently, Again the solvent in gas is condensed out by condensation separator 40.The solvent for condensing out enters into condensate tank 50.It is cold Solidifying separator 40 can further connect ethene collection device, such as cryogenic separation device, and gas is again through depth refrigerated separation Product ethene is obtained.

Entered into by liquid outlet in filter plant 70 in the solvent of reactor bottom, catalyst is filtered from solvent Out.Solvent after filtration is entered in green oil removing system 80, is removed system 80 by green oil and is separated green oil with solvent, molten Agent enters back into solvent heater 20, and green oil is then preserved into green oil storage tank.It is heated change in the internal solvent of solvent heater 20 Into after steam, enter in reactor from the steam inlet of reactor bottom.The catalyst filtered out from filter plant 70 is then It is added in condensate tank 50.

In condensate tank 50, after by agitating device catalysts and solvents are well mixed, then by solvent pump 60 Mixed liquid is sent in reactor.The process is capable of achieving recycling for catalyst.

In the present embodiment, the solvent for using is distilled water (5 μm/cm of electrical conductivity ＜).Rise from reactor bottom Steam is the thermal source of whole reactor, keeps the relatively stable of system temperature.When selective hydrogenation of acetylene reaction is started, release Substantial amounts of heat can be shifted by the evaporation of solvent, it is to avoid there is the too high phenomenon of local temperature in reactor.

Solvent heater in the utility model can be using electrical heating, steam heating, flue gas or heat-conducting oil heating Mode realizing.

Compared with the technology of a small amount of acetylene hydrogenation in current ethene, this technology can be realized being added by high concentration selective acetylene Hydrogen ethene, has further expanded the technology path of Coal Chemical Industry.

Further, in technical solutions of the utility model, gas be to it is lower and on flow direction, liquid is from top to down Flow direction, gas phase and liquid phase integrally present the direction of adverse current, increase the effect of mass transfer and heat transfer.

Further, there is multiple sieve plate in the reactor of the technical solution of the utility model, that is, mean reactor In there are multiple little paste state bed reactors, increase the contact area that gas-liquid-solid three-phase is fully contacted, improve gas-liquid flow Field distribution, can avoid short circuit, but also can strengthen turbulence and gas-liquid mass transfer, improve the quality of fluidisation in reactor.

Further, green oil removing system is provided with system of the present utility model, green oil is significantly reduced to reaction Impact, realize the smooth long term running of device；The solvent for using in solvent heater simultaneously is to remove the solvent after green oil, Heat can be saved, and avoids local temperature in reactor too high.

System of the present utility model enables catalyst to recycle, and improves the utilization ratio of catalyst.

The technical solution of the utility model using liquid phase solvent sensible heat (sensible heat referred to after this heat is added or removed, The change of mass temperature can be caused, and do not undergone phase transition), heat-sinking capability is significantly improved, and can be quickly moved out because of selective acetylene The heat for being hydrogenated to ethene and producing, reduces the temperature of reaction bed, improves the conversion ratio of acetylene and the selectivity of ethene.

In addition, the heating system of the technical program is simple, only relies on the solvent heater outside reactor and can be realized as Heat supply.

In a word, the reaction system that the utility model is provided, when carrying out selective hydrogenation of acetylene reaction, can be effectively prevented from There is " temperature runaway " phenomenon, can in time remove green oil, can preferably suppress during preparation of ethylene through selective hydrogenation of acetylene because heat release is anti- The appearance of focus in the beds answered and cause, and then avoid catalyst from inactivating, improve the stability of catalyst.This practicality The equipment of new proposition solves the problems, such as well that catalyst use efficiency is low by the way of catalyst recycling.

Embodiment 1

The system for preparing ethylene by selective hydrogenation of acetylene in using embodiment is as shown in Figure 3.System architecture is as above State the form described in embodiment.The operating pressure of the system is 0.25MPa, and temperature is 130 DEG C.Nitrogen conduct can first be used The solvent containing catalyst in source of the gas, with paste state bed reactor sets up gas-liquid flow direction；Subsequently, then gradually solvent heater is opened (pressure in solvent heater is 0.27MPa), sets up steam ascending air.Cool back when steam rises to reactor head Stream, and after temperature stabilization, nitrogen can be gradually converted to hydrogen and the gaseous mixture of acetylene gas is passed in the middle of reactor. In the reactor, acetylene and hydrogen generate ethene under the catalytic action of catalyst；Reacted gas passes through again condenser 30 With condensation separator 40, after the solvent in gas is condensed out, then reaction system battery limit (BL) is sent.From reactor top with solvent stream To the catalyst of reactor bottom, then filtered out by filter plant 70, then transferred in the middle of condensate tank 50. After solvent and catalyst are well mixed in condensate tank 50, using solvent pump by catalyst transport to reactor head.Filter Solvent afterwards is entered in green oil removing system 80, is removed system 80 by green oil and is separated green oil with solvent, and solvent is entered back into To solvent heater 20；After the internal solvent of solvent heater 20 is heated and becomes steam, from the solvent vapo(u)r entrance of reactor bottom Enter in reactor.

In the present embodiment, the solvent for using is distilled water (5 μm/cm of electrical conductivity ＜), enters anti-from solvent heater The steam for answering the rising of device is the thermal source of whole reactor, keeps the relatively stable of system temperature.Add when selective acetylene is started When hydrogen reacts, the substantial amounts of heat of releasing can be shifted by the evaporation of solvent, it is to avoid local temperature is too high.What is used urges The particle diameter of agent is 40-150 μm, and the filtering accuracy of the filter plant for using is 1 μm.

Finally it should be noted that：Obviously, above-described embodiment is only intended to clearly illustrate the utility model example, And not to the restriction of embodiment.For those of ordinary skill in the field, may be used also on the basis of the above description To make other changes in different forms.There is no need to be exhaustive to all of embodiment.And thus Among the obvious change amplified out or variation are still in protection domain of the present utility model.

Claims (8)

1. the reaction system for preparing ethene of a kind of external heat, it includes：It is paste state bed reactor, condenser, condensation separator, cold Lime set storage tank, solvent pump, filter plant, green oil removing system and solvent heater；

Wherein described paste state bed reactor includes housing and sieve plate,

The bottom of the housing is provided with reaction gas inlet, solvent vapo(u)r entrance, liquid outlet；The top of the housing is provided with gas Body is exported and liquid inlet；

The sieve plate is located in the housing, is fixed in the inner walls, under the liquid inlet, the reaction On gas access, the solvent vapo(u)r entrance；

The solvent heater is connected by the solvent vapo(u)r entrance with the paste state bed reactor, and the filter plant passes through The liquid outlet is connected with the paste state bed reactor, and the condenser is by the gas vent and the slurry reactor Device is connected, and the solvent pump is connected by the liquid inlet with the paste state bed reactor；

The condenser, the condensation separator, the condensate tank and the solvent pump are sequentially communicated；The filter plant Connect with the condensate tank；The filter plant, green oil removing system and the solvent heater are sequentially communicated.

2. system according to claim 1, it is characterised in that be provided with agitating device in the condensate tank.

3. system according to claim 1, it is characterised in that the condensation separator connects ethene collection device.

4. system according to claim 1, it is characterised in that be dispersed with multilayer inside the paste state bed reactor and mutually put down Capable sieve plate, spaced between the sieve plate of adjacent layer, the interval of each layer sieve plate is equal.

5. system according to claim 1, it is characterised in that per layer of sieve plate includes seal pot, bubbling area, downflow weir And downspout；Wherein, the part edge of the sieve plate is fixed with the inner walls；

The part that the part edge of the fixation fences up with the downflow weir is seal pot, for holding from descending liquid described in upper strata The liquid that pipe is flowed down；

The centre of the seal pot is distributed with sieve aperture, forms bubbling area, and the bubbling area is the main region of gas liquid reaction； The downflow weir is located at revocable edge of the sieve plate, and the downflow weir is higher than the seal pot of place layer, for keeping every The height of liquid on the layer sieve plate；

The downspout is used to make the downflow weir of sieve plate described in liquid from upper strata to flow to the seal pot of sieve plate described in lower floor, positioned at institute State the side of downflow weir.

6. system according to claim 5, it is characterised in that the sieve aperture is equally distributed circular aperture, described little The centre-to-centre spacing in hole is 1-5 times of aperture, a diameter of 5-20mm of the aperture.

7. system according to claim 5, it is characterised in that the sieve aperture of the sieve plate is provided with float valve or bubble-cap.

8. system according to claim 5, it is characterised in that the bottom of the downspout of sieve plate described in upper strata is not higher than lower floor The height of the sieve plate downflow weir.