CN206045989U - A kind of response system of utilization prepared in slurry bed reactor for ethylene - Google Patents
A kind of response system of utilization prepared in slurry bed reactor for ethylene Download PDFInfo
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- CN206045989U CN206045989U CN201620580511.XU CN201620580511U CN206045989U CN 206045989 U CN206045989 U CN 206045989U CN 201620580511 U CN201620580511 U CN 201620580511U CN 206045989 U CN206045989 U CN 206045989U
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Abstract
This utility model is related to a kind of response system of utilization prepared in slurry bed reactor for ethylene.System includes：Paste state bed reactor, condenser, condensation separator, condensate tank, solvent pump, bottom of towe solvent tank, filter plant, green oil removing system, high-temperature heating equipment and catalyst reduction device；Paste state bed reactor includes housing, heater and sieve plate；The bottom of housing is provided with reaction gas inlet, liquid flux entrance, liquid outlet；The top of housing is provided with gas outlet and liquid inlet；Heater is arranged on the bottom in housing；Sieve plate is located in housing, is fixed in inner walls.This utility model can effectively solving prior art prepare ethylene so that internal heat is difficult the problem for spreading out of, catalyst utilization is low.
Description
Technical field
This utility model generally relates to the preparation field of ethylene, and in particular to a kind of to utilize prepared in slurry bed reactor for ethylene
Response system.
Background technology
One of ethylene is a kind of important basic material in modern industry, and the maximum chemicals of world wide production, its product
Product are widely used in the fields such as national economy, people's lives, national defence, are " mothers of organic synthesiss ".In the face of the shortage of petroleum resources
Soaring with international oil price, raw material sources become the bottleneck of development ethylene industry, and asking of must solving in face of people of pendulum
Topic.Therefore, research and develop a kind of new Technology to prepare ethylene, to be allowed to petroleum replacing as industrial raw materials, can
Alleviate dependency of the modern industry to oil.
In coal chemical technology, pass through Non-catalytic partial by 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, develop the new technology of producing ethylene with acetylene hydrogenation
Technology, has broad application prospects.
Low concentration acetylene gas and solid phase catalyzing hydrogen addition technology is highly developed in the oil industry, removes in being mainly used in ethylene
Acetylene impurities, the reactor for using are fixed bed reactors, and loading solid-phase catalyst in the reactor carries out gas-solid phase reaction.But
As 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 ".
Fluidized-bed process and device of the prior art one for a kind 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 ethylene；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 cooling medium is to remove during reaction in the process
The substantial amounts of heat released, but still it is difficult to 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 ethylene, including oxygen hydrogenation reactor, the second exsiccator of cracking gas,
Removal of mercaptans/cos reactor, dearsenization 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 ", fundamentally improves gas-liquid flow field distribution, improves the quality of fluidisation in reactor, it is necessary to propose
A kind of new response system for preparing ethylene.
Utility model content
The purpose of this utility model is the response system for providing a kind of utilization prepared in slurry bed reactor for ethylene, to solve
Prior art prepares ethylene so that internal heat is difficult the problem for spreading out of, catalyst utilization is low.
This utility model provides a kind of response system of utilization prepared in slurry bed reactor for ethylene, and which includes：Slurry bed system is anti-
Answer device, condenser, condensation separator, condensate tank, solvent pump, bottom of towe solvent tank, filter plant, green oil removing system,
High-temperature heating equipment and catalyst reduction device；Wherein described paste state bed reactor includes housing, heater and sieve plate；The shell
The bottom of body is provided with reaction gas inlet, liquid flux entrance, liquid outlet；The top of the housing is provided with gas outlet and liquid
Body entrance；The heater is arranged on the bottom in the housing；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 liquid flux entrance；The green oil takes off
Except system is connected with the paste state bed reactor by the liquid flux entrance, the bottom of towe solvent tank passes through the liquid
Outlet is connected with the paste state bed reactor, and the condenser is connected with the paste state bed reactor by the gas outlet,
The solvent pump is connected with the paste state bed reactor by the liquid inlet；The condenser, the condensation separator, institute
State condensate tank and the solvent pump is sequentially communicated；The bottom of towe solvent tank, the filter plant, high-temperature heating dress
Put, the catalyst reduction device and the condensate tank are sequentially communicated；The filter plant removes system with the green oil
Connection.
Above-mentioned system, is provided with agitating device in the condensate tank.
Above-mentioned system, the condensation separator connect ethylene collection device.
Above-mentioned system, is dispersed with the sieve plate that multilamellar 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 include 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 is fenced up with the downflow weir is by liquid
Disk；For holding from downspout described in upper strata the liquid for flowing down；The centre of the seal pot is distributed with sieve aperture, forms bubbling
Area, the bubbling area are the main regions of gas liquid reaction；The downflow weir is located at revocable edge of the sieve plate, described to overflow
Seal pot of the stream weir higher than 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 are 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 are provided with float valve or bubble-cap.
Above-mentioned system, the bottom of the downspout of sieve plate described in upper strata are not higher than the height of sieve plate downflow weir described in lower floor.
The beneficial effects of the utility model are, the utility model proposes a kind of new utilization prepared in slurry bed reactor is standby
The response system of ethylene, the response system are simple to operation, and course of reaction is easily achieved shifting heat, catalyst reusable edible, energy
Enough removing green oils in time so that carrying out high concentration selective hydrogenation of acetylene using paste state bed reactor becomes a kind of important alkene processed
The production ways of hydrocarbon.
Description of the drawings
Fig. 1 prepares the structural representation of the paste state bed reactor of ethylene 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 structure schematic flow sheet that technical solutions of the utility model embodiment prepares ethylene.
Specific embodiment
Below in conjunction with drawings and Examples, specific embodiment of the present utility model is described in more details, with
Just better understood when the advantage of scheme of the present utility model and its various aspects.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 this utility model.Wherein：1st, reaction gas inlet；2nd, liquid
Outlet；3rd, gas outlet；4th, liquid inlet；5th, sieve plate；6th, downspout；7th, heater；8th, solvent liquid entrance.
The principle of paste state bed reactor is gas with bubbling form by being suspended with liquid (serosity) layer of solid fine grain, with
Realize the reactor of gas-liquid solid state 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, heater 7 and sieve plate 5.
Reactor shell bottom is provided with reaction gas inlet 1, solvent liquid entrance 8 and liquid outlet 2, reactor shell
Gas outlet 3 is arranged at top.
In the bottom having heaters 7 of reactor, which is penetrated in reactor enclosure body.Wherein, heater 7 steams can solvent
Send out, there is provided the continuous steam air-flow for rising, while providing thermal source for whole reactor.
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 liquid flux entrance 8.
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 is fenced up with the downflow weir is seal pot, for holding from upper strata downspout the liquid for flowing down.
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 5 downflow weir of lower floor's sieve plate.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, is uniform-distribution with circular aperture 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
Contact into bubbling.
The response system for ethylene using prepared in slurry bed reactor is illustrated in figure 3, what which was mentioned in including described above
Paste state bed reactor 10, condenser 30, condensation separator 40, condensate tank 50, solvent pump 60, bottom of towe solvent tank 70, mistake
Filter equipment 80, green oil removing system 90, high-temperature heating equipment 100 and catalyst reduction device 110.Green oil removing system 90 passes through
The liquid flux entrance is connected with the paste state bed reactor 10, the bottom of towe solvent tank 70 by the liquid outlet with
The paste state bed reactor 10 is connected, and the condenser 30 is connected with the paste state bed reactor 10 by the gas outlet,
The solvent pump 60 is connected with the paste state bed reactor 10 by the liquid inlet；The condenser 30, the condensation point
It is sequentially communicated from device 40, the condensate tank 50 and the solvent pump 60；The bottom of towe solvent tank 70, the filter plant
80th, the high-temperature heating equipment 100, the catalyst reduction device 110 and the condensate tank 50 are sequentially communicated, catalyst
Pass sequentially through the said equipment；The paste state bed reactor 10, the bottom of towe solvent tank 70, the filter plant 80 are green with described
Oily removing system 90 is connected, and solvent passes sequentially through the said equipment.
Above-mentioned system, is provided with agitating device in the condensate tank 50, for solvent in condensate tank 50 with urge
The stirring of agent.
When preparing ethylene, the gaseous mixture of acetylene and hydrogen is entered by the reaction gas inlet 1 of 10 bottom of paste state bed reactor
Enter in reactor；Reacting gas with solvent vapo(u)r together by the aperture on the sieve plate of inside reactor enter into liquid phase it
In.Wherein solvent vapo(u)r generates liquid flux heating evaporation by the heater 7 of reactor bottom.Catalyst and carrier solvent
Flow in the liquid inlet 4 on autoreactor top.Because aperture is equally distributed on sieve plate 5, so reacting gas is also therewith
Evenly spread in the middle of liquid.In a liquid, reacting gas occurs under the catalytic action of the catalyst being suspended in liquid instead
Should.Reacted gas departs from this layer of sieve plate 5, then is entered in the middle of supernatant liquid by the aperture of upper strata sieve plate 5.So repeatedly
Until the sieve plate 5 by reactor the top, goes out from the gas outlet 3 of reactor top.
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, is improved gas-liquid
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,
The solvent in gas is condensed out by condensation separator 40 again.The solvent for condensing out enters into condensate tank 50, gas
Body is obtained product ethylene through depth refrigerated separation again.
Bottom of towe solvent tank 70 is entered into by liquid outlet in the solvent of reactor bottom, then by filter plant 80,
Catalyst after filtration is capable of the green oil of effective Removal of catalyst surface attachment again after the calcining of high-temperature heating equipment 100
With the impurity such as solvent, the regeneration of catalyst is realized.But the catalyst after calcination is oxidation state, therefore to fill through catalyst reduction
Put 110 to realize the reduction of catalyst.Catalyst after reducing/regenerating adds into condensate tank 50 again.And filter out
Solvent is then entered in green oil removing system 90.System 90 is removed by green oil green oil is separated with solvent, solvent is by reaction
The liquid inlet of device bottom is returned to reactor, and green oil is then preserved into green oil storage tank.
In condensate tank 50, after agitating device is by catalysts and solvents mix homogeneously, 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.
Heater in this utility model can use the side of electrical heating, steam heating, flue gas or heat-conducting oil heating
Formula is realizing.
High-temperature heating equipment in this utility model can come real using heaters such as electrical heating, revolving bed, fluid beds
It is existing.
Compared with the technology of a small amount of acetylene hydrogenation in current ethylene, this technology can be realized being added by high concentration selective acetylene
Hydrogen ethylene, 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 area that gas-liquid-solid three-phase is fully contacted, improve gas-liquid flow field point
Cloth, 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 and catalyst regeneration system is provided with system, significantly reduce green oil and
Catalyst activity reduces the impact to reacting, and realizes the smooth long term running of device；While system of the present utility model and side
Method 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 ethylene and producing, reduces the temperature of reaction bed, improves the selectivity of the conversion ratio and ethylene of acetylene.
In addition, the heating system of the technical program is simple, the heater for only relying on reactor bottom can be realized as heat supply.
In a word, the response system that this utility model is provided, when carrying out selective hydrogenation of acetylene reaction, can be effectively prevented from sending out
Raw " temperature runaway " phenomenon, can preferably suppress the beds caused because of exothermic reaction during preparation of ethylene through selective hydrogenation of acetylene
The appearance of middle focus, can remove green oil in time, it is to avoid catalyst is inactivated, and improve the stability of catalyst.This utility model is carried
The equipment for going out solves the problems, such as that by the way of catalyst recycling catalyst use efficiency is low well.
Embodiment 1
The system for preparing ethylene by selective hydrogenation of acetylene in using embodiment is as shown in Figure 3.System structure is as above
State the form described in embodiment.The operating pressure of the system is 0.25MPa, and temperature is 130 DEG C.
The solvent containing catalyst during nitrogen can first be used as source of the gas, with paste state bed reactor 10 sets up gas-liquid flow direction；
Subsequently, then gradually the heater of bottom is opened, steam ascending air is set up.When steam rises to reactor head cooling for reflux,
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 ethylene under the catalytic action of catalyst；Reacted gas passes through again
Condenser 30 and condensation separator 40, after the solvent in gas is condensed out, then send response system battery limit (BL).Condensation separator
40 can further connect ethylene collection device, and such as cryogenic separation device obtains ethylene product.
The catalyst of reactor bottom is flow to solvent from reactor head, then is filtered out by filter plant 80；When
It was found that when catalyst activity is reduced, catalyst is passed sequentially through 110 groups of high-temperature heating equipment 100 and catalyst reduction device
Into catalyst regeneration system, realize the regeneration of catalyst；Then the catalyst after regeneration is transferred to into condensate tank 50 again
It is central；After mix homogeneously in condensate tank 50, reactor head is transported to using solvent pump 60.When in discovery solvent
Green oil amount increase, when reducing reactivity, can by the solvent filtered out from filter plant 80 be passed into green oil removing system
In system 90, green oil therein is removed.Green oil removes system 90 and catalyst regeneration system significantly reduces green oil and catalyst
Activity reduces the impact to reacting, and realizes the smooth long term running of device.
In the present embodiment, the solvent for using is distilled water (5 μm/cm of electrical conductivity ＜), from the steaming that reactor bottom rises
Vapour is the thermal source of whole reactor, keeps the relatively stable of system temperature.When selective hydrogenation of acetylene reaction is started, releasing
Substantial amounts of heat, can be shifted by the evaporation of solvent, it is to avoid local temperature is too high.The particle diameter of the catalyst for using is 40-
150 μm, 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 this utility model example,
And the not restriction to 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
It is amplified obvious change or change still in protection domain of the present utility model among.
Claims (8)
1. response system of a kind of utilization prepared in slurry bed reactor for ethylene, which includes：Paste state bed reactor, condenser, condensation
Separator, condensate tank, solvent pump, bottom of towe solvent tank, filter plant, green oil remove system, high-temperature heating equipment and urge
Agent reduction apparatus；
Wherein described paste state bed reactor includes housing, heater and sieve plate,
The bottom of the housing is provided with reaction gas inlet, liquid flux entrance, liquid outlet；The top of the housing is provided with gas
Body is exported and liquid inlet；
The heater is arranged on the bottom in the housing；
The sieve plate is located in the housing, is fixed in the inner walls, under the liquid inlet, the reaction
On gas access, the liquid flux entrance；
The green oil removing system is connected with the paste state bed reactor by the liquid flux entrance, the bottom of towe solvent storage
Tank is connected with the paste state bed reactor by the liquid outlet, and the condenser is by the gas outlet and the slurry
Bed reactor connection, the solvent pump are connected with the paste state bed reactor by the liquid inlet；
The condenser, the condensation separator, the condensate tank and the solvent pump are sequentially communicated；The bottom of towe solvent
Storage tank, the filter plant, the high-temperature heating equipment, the catalyst reduction device and the condensate tank connect successively
It is logical；The filter plant removes system connectivity with the green oil.
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 ethylene collection device.
4. system according to claim 1, it is characterised in that be dispersed with multilamellar 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 is fenced up with the downflow weir is seal pot, for holding from descending liquid described in upper strata
Liquid under pipe flow；
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, seal pot of the downflow weir higher than place layer, for keeping every
The height of liquid on the layer sieve plate；
The downspout is used for the seal pot for making the downflow weir of sieve plate described in liquid from upper strata flow to 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
1-5 times for aperture of the centre-to-centre spacing in hole, 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.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105879792A (en) * | 2016-06-14 | 2016-08-24 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene by means of slurry bed reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105879792A (en) * | 2016-06-14 | 2016-08-24 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene by means of slurry bed reactor |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
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| CP01 | Change in the name or title of a patent holder |
Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee after: Shenwu Technology Group Co.,Ltd. Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee before: BEIJING SHENWU ENVIRONMENT AND ENERGY TECHNOLOGY Co.,Ltd. |
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| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: Reaction system and method for preparing ethylene by means of slurry bed reactor Effective date of registration: 20180330 Granted publication date: 20170329 Pledgee: Tianfeng Securities Co.,Ltd. Pledgor: Shenwu Technology Group Co.,Ltd. Registration number: 2018990000247 |
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