CN107324966A - The preprocess method and its device of product gas in oxygenatedchemicals olefin process - Google Patents

The preprocess method and its device of product gas in oxygenatedchemicals olefin process Download PDF

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CN107324966A
CN107324966A CN201710580268.0A CN201710580268A CN107324966A CN 107324966 A CN107324966 A CN 107324966A CN 201710580268 A CN201710580268 A CN 201710580268A CN 107324966 A CN107324966 A CN 107324966A
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gas
phase
catalyst
filter
reactor
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蒋斌波
陆飞鹏
王靖岱
廖祖维
黄正梁
阳永荣
周冰洁
席志祥
柴宇伦
周立进
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Zhejiang University ZJU
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    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00Purification; Separation; Use of additives
    • C07C7/005Processes comprising at least two steps in series
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00Purification; Separation; Use of additives
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of bulk chemicals

Abstract

The invention discloses the preprocess method and its device of product gas in a kind of oxygenatedchemicals olefin process.The present invention passes sequentially through cyclone separator, filter, depickling reactor by using by reactor outlet product gas, and reclaim heat through heat exchanger, sent into after cooling again through air cooler and gas phase, aqueous phase and oil-phase product are obtained after three phase separator condensation, wherein gas-phase product feeding separation of olefins unit.The present invention can effectively solve catalyst fines and organic acid etching problem, simplify oxygenatedchemicals olefine reaction flow, so as to not only realize the stable operation of commercial plant, and realize the target for saving equipment investment and energy-saving and emission-reduction.

Description

The preprocess method and its device of product gas in oxygenatedchemicals olefin process
Technical field
The invention belongs to alkene preparing technical field, it is related to one kind with oxygenatedchemicals(Mainly include methanol, ethanol, two Methyl ether, C4-C10 alcohol compounds or its mixture)Reaction in the tandem reaction sequence of alkene is generated for raw material and generates the pre- of gas Processing system.
Background technology
Low-carbon alkene, refers to ethene and propylene, is important basic petrochemical raw material, and it is mainly derived from the catalysis of crude oil Cracking and the steam cracking of naphtha.And above-mentioned traditional petroleum base route prepares low-carbon alkene and does not meet China's " many coals The energy resource structure of few gas ".Therefore, develop relatively independent ethene, production of propylene technology turns into domestic and international development of chemical industry Active demand.
Take the oxygenatedchemicals represented as raw material production low-carbon alkene, such as methanol-to-olefins of methanol or dimethyl ether (Methanol to Olefin, MTO) and preparing propylene from methanol (Methanol to Propylene, MTP) technology, is not only solved Petrochemical materials ethene and propylene carry out source problem, while also widened the downstream industry chain of ammonia from coal, and successfully Coal chemical industry and petrochemical industry are closely connected, with important economy and industrial application value.At present, fluidized-bed reactor Occupied an leading position in MTO and MTP technologies is the oxygenatedchemicals alkene technologies of representative.
In order to obtain purer olefin product gas, oxygen-containing organic compound propylene reaction gas is carrying out lighter hydrocarbons separation Before need to be pre-processed.For example, can a small amount of organic acid of by-product, the presence of these organic acids in oxygenatedchemicals olefin hydrocarbon Detrimental effect can be brought to downstream process, it is necessary to take corresponding pretreatment.In addition, for fluidized-bed reactor, by Fluidized in the reactor in molecular sieve catalyst under continuous working condition, the severe friction between catalyst can cause catalysis The generation of agent fine powder, if untreated can cause the blocking of follow-up heat transmission equipment and separation equipment.In addition, catalyst fines are not The loss that will also result in a large amount of catalyst is received in add-back.
US 4338475 discloses a series of equipment that the oxygenatedchemicals such as methanol are converted into hydro carbons in fluid bed.Its In, separated by the fine powder for generation of being worn and torn in setting three-stage cyclone separator to reactor on fluid bed top.But due to Catalyst fines size is small, weight is low, therefore Cyclone efficiency is relatively low, several especially for the fine powder less than less than 5 μm It can not handle, therefore still have a large amount of catalyst fines and enter follow-up equipment, influence device stable operation.
US 6459009 is disclosed reclaims oxygenatedchemicals converted olefin water in products and heat using two-stage chilling Tower System The technology of amount.First order chilling tower is mainly used in partially recycled product moisture, while the heat reclaimed can meet the preheating of raw material. First order chilling top of tower logistics area sends into second level chilling tower, due to the recovered most impurity of first order chilling tower With high boiling oxygenatedchemicals, therefore need to only to lead to too small amount of vapor air lift higher with regard to that can obtain purity for second level chilling tower Water.The technology can not only separate a large amount of impurity, and reduce investment reduction energy consumption.However, the technology is not directed to point The process problem of Catalyst Adsorption in chaotropic phase, and due to the presence of organic acid in product, the corrosivity of liquid phase in chilling tower Also do not consider.
CN101544529B discloses a kind of reaction produced gas in olefin preparation technology by oxygen-containing compounds preprocess method and equipment. For existing oxygenatedchemicals olefine reaction generation temperature degree it is higher, and containing a small amount of catalyst shortcoming, by product gas according to It is secondary to be passed through the catalyst dust that chilling tower, water scrubber to carry in washing reaction generation gas, while at utmost reduction reaction life Into the temperature of gas, high temperature heat is reclaimed.The water that chilling and washing equipment are used is respectively from chilling bottom of towe and water scrubber bottom water, no Other cooling mediums are needed, while the low temperature heat energy of chilling bottom of towe and water scrubber bottom water can be reclaimed, the energy consumption of device are reduced.But The preprocess method does not consider that the organic acid composition in reaction generation gas can cause etching problem to equipment.In addition, containing big There is also very big problem for the processing of the bottom of towe cooling water of amount catalyst fines.
A kind of method that CN201010116429.9 discloses removing and recycle-water in oxygenatedchemicals olefin stream, it is main Solve conventional art and equipment blocking is easily caused during a large amount of water contained by oxygenatedchemicals producing olefinic hydrocarbons logistics are reclaimed The problems such as corrosion.The technology carries out catalyst fines, organic acid removing stage by stage by fast cooling device, and in separation product Water, is prevented effectively from equipment scaling, blocks and corrode, reduce wastewater treatment load.However, the patent does not account for chilling operation Middle alkaline cleaning can cause the loss of oxygenatedchemicals to increase, and the process is whard to control.Meanwhile, condensed water is individually located in batches The problem of there is big equipment investment and complicated operating process in reason.
CN104725181B discloses a kind of first separating technology of oxygenatedchemicals propylene reaction generation gas, and the technology is carried Go out by depickling reactor and pair set in follow-up refrigerating work procedure to solve oxygenatedchemicals propylene gas product in the prior art The problem of standby corrosion.But the problem of technology does not consider to carry big catalyst fines secretly in fluidized-bed process, if be introduced directly into Depickling reactor can cause depickling activity is rapid to decline due to catalyst fines adhesion.In addition, the fine powder of entrainment can similarly be led Cause follow-up heat exchange and separation equipment to block, influence the operation stability of whole device.
In fact, the high-temperature gas generated for oxycompound olefine reaction contains a large amount of heat energy, existing procedure is By chilling means by reacting gas from more than 200 DEG C of High-temperature cooling to less than 100 DEG C, cause a large amount of 100 DEG C it is higher above The waste of potential temperature heat resource.Cause the high temperature heat wasting of resources main reason is that contains micro organic acid in reaction product, Easily cause equipment corrosion., can etching apparatus if reacting gas separates out liquid in cooling procedure.Existing procedure is to avoid acid Property corrosion, using in chilling tower plus in the method for alkali lye and organic acid, but chilling means cause energy loss in flow excessive. In addition, if the catalyst fines carried secretly with reaction product stream can not be removed timely and effectively, can cause follow-up heat exchange and The fouling and blocking of separation equipment, cause whole technique pressure drop rise.The catalyst particle deposition washed using chilling tower Be suspended in bottom of towe water, can also produce a large amount of technique waste waters, and it is difficult to cause catalyst fines to reclaim.Therefore, how to close Catalyst fines in the solution sour corrosion of reason, removing product gas, and the high temperature heat that generation gas is carried is reclaimed, for maintaining All have great importance in terms of the long-term operating of oxycompound olefin hydrocarbon apparatus and process economy and energy-saving and water-saving.
The content of the invention
The technical problems to be solved by the invention are oxygenatedchemicals olefin process, particularly fluid bed in conventional art The problem of entrained catalyst particles or fine powder are difficult to separate and reclaimed in product gas in technique, and by-product is organic in product gas Acid causes follow-up heat returnable bottle neck and equipment corrosion problem.The present invention provides product in a kind of oxygenatedchemicals olefin process The pretreatment system of gas, the system can effectively remove the catalyst fines in oxygenatedchemicals conversion process in product gas first, So as to avoid blockage problem caused by catalyst fines are accumulated in follow-up heat recovery and separation equipment.Secondly, the technique Depickling reactor is also introduced, and loads special-shaped protective agent and catalyst, cyclone separator can be not only eliminated and filter difficulty or ease is removed Most catalyst fines(Particle diameter is less than 5 μm), and organic acid composition in selectively removing product gas, thus fundamentally solve Fine powder is blocked and organic acid corrosion problem.Finally, the elimination based on dew point corrosion, passes through the product gas after gas solid separation, depickling Energy regenerating is carried out, abandoning tradition chilling tower, water scrubber mode are realized that the high efficiente callback of high-temperature product gas heat is utilized, realized The target of energy-saving and water-saving.
The preprocess method of product gas in a kind of oxygenatedchemicals olefin process that the present invention is provided, including following step Suddenly:
(1)The obtained high temperature hydrocarbon product gas of oxygenatedchemicals conversion first passes around cyclone separator, for initial gross separation and returns Receive catalyst fines in product;
(2)The product gas feeding filter of Cyclone outlet is thin for further separating and reclaiming catalyst in product gas Powder;
(3)The gas of filter outlet enters depickling reactor, for removing corrosive organic acid component in product gas;
(4)The exit gas of depickling reactor reclaims heat by heat exchanger, then sends into three phase separator after cooling through air cooler Gas phase, aqueous phase and oil-phase product, wherein gas-phase product feeding separation of olefins unit are obtained after condensation.
Described cyclone separator is multi-cyclone, including two or more cyclone separators.
Described filter is in glass fiber filter, woven wire sintered filter core filter, electric precipitation filter One or more.
Described heat exchanger includes heat exchanger in series or in parallel.
Described depickling reactor is fixed bed reactors, and it is at the middle and upper levels deacidifying catalyst, and lower floor is protective agent, depickling Catalyst and protective agent are shaped as cylinder, gear shape, cloverleaf pattern, porous ball, cellular or bird-nest-shaped.
Catalysts are 0.5 ~ 10 with deacidifying catalyst mass ratio, and deacidifying catalyst loads height ratio with protective agent and is 0.1~10。
Organic acid total content is less than 30 ppm in the exit gas product of described depickling reactor.
Described three phase separator inlet temperature is 40 ~ 80 DEG C.
The present invention also provides a kind of device of product gas preprocess method in use oxygenatedchemicals olefin process, and it is special Levy and be, including reactor, regenerator, cyclone separator, filter, depickling reactor, heat exchanger, air cooler, three phase separation Device, compression machine, gas-liquid separator;Oxygenatedchemicals is carried out in the reactor, and the catalyst inactivated after reaction is in a regenerator From regenerator top and by cyclone separator gas-particle separation occurs for regeneration, reaction gas, and most of catalyst fines are by whirlwind point Caught from device, Cyclone outlet reaction gas is sent directly into filter, chi is caught by the filled by filtration material in filter Very little less catalyst fines, filter outlet gas enters depickling reactor, and passes sequentially through protective agent and beds, Depickling reactor outlet high-temperature gas reclaims heat through multi-stage heat exchanger, and three phase separator is sent into after then cooling again through air cooler The oily three phase separation of gas-liquid is carried out, wherein isolated aqueous phase carrying device, and the compressed machine of gas-phase product, gas-liquid separator Contact and redistribute again with oil-phase product afterwards, the gas phase and liquid product formed respectively goes out device.
Compared with prior art, the present invention can effectively solve catalyst fines and organic acid etching problem, and simplification is oxygen-containing Compound olefine reaction flow, so as to not only realize the stable operation of commercial plant, and realizes saving equipment investment and section The target of energy emission reduction, in terms of the prominent beneficial effect of the present invention is mainly reflected in three below:
(1)The preprocess method and its device proposed in the technology of the present invention can effectively solve the problem of catalyst fines are brought, special It is not the catalyst fines for solving size below 5 μm;
(2)Depickling is directly carried out to high-temperature product gas, etching problem of the organic acid composition to follow-up equipment is fundamentally solved;
(3)The power recovery scheme of high-temperature product gas is simplified, equipment investment is reduced, while energy-saving and water-saving can be realized.
Brief description of the drawings
Fig. 1 is the preprocess method of product gas in oxygenatedchemicals olefin process and its schematic diagram of device;
Fig. 1:1- reactors, 2- regenerators, 3- cyclone separators, 4- filters, 5- depickling reactors, 6- heat exchangers, 7- air coolings Device, 8- three phase separators, 9- compression machines, 10- gas-liquid separators, wherein omitting all pumping units.
Embodiment
The present invention is further explained in detail by the description below with reference to accompanying drawing, but following description is only used for making skill of the present invention The those of ordinary skill in art field can be more clearly understood from the principle and marrow of the present invention, be not meant to progress of the present invention Any type of limitation.
Generally, through arranging multi-cyclone to urging for being carried in exported product gas in the expanding reach of MTO reactors top Agent fine powder is separated.Usually, three-stage cyclone separator catalyst at inlet concentration of solid particles is 800 ~ 900 mg/m3, And the concentration in three-stage cyclone separator exit is reduced to 150 ~ 300 mg/m3, it is meant that about 60 ~ 85 volume % catalyst fines are obtained To separation.As can be seen here, multi-cyclone can separate most of catalyst fines from product gas.However, rotation The not treatable catalyst fines particle diameter of wind separator is approximately less than 10 μm, and volume ratio accounts for more than 99%, wherein absolutely mostly Number is less than 5 μm of catalyst granules for particle diameter, accounts for catalyst fines cumulative volume about 85% ~ 90%.And this partial catalyst fine powder It is the major reason for causing follow-up equipment to block.
In addition, generally product gas enters chilling tower, bottom of towe condensed water small molecular organic acid content model after heat recovery 50ppm ~ 300ppm is trapped among, pH scopes are between 3.7 ~ 5 scopes.This has resulted in the etching problem of fast cooling device.Technique is containing acid The traditional processing mode of water is to add certain density NaOH by measuring pump to neutralize, and the pH of control chilling water system is more than 7, letter Claim chilling alkali washing process.Alkali lye is often injected in actual production process can cause the pH fluctuations of system larger, sometimes even small In 5, this will cause corrosion to system equipment.And injecting more NaOH can damage to tower wall, shorten tower wall and use the longevity Life.Further, since there is organic acid and in order to avoid it corrodes in dew point, reaction gas in conventional methanol olefin process After heat exchange washing separation is carried out to 190 DEG C or so i.e. feeding chilling towers.As can be seen here, the presence of organic acid dew piont corrosion bottleneck Also the heat recovery of high-temperature product gas is constrained, is unfavorable for reducing process energy consumption.
As shown in figure 1, oxygenatedchemicals is carried out in reactor 1, the catalyst inactivated after reaction in regenerator 2 again Give birth to, therefore catalyst is circulated between reactor 1 and regenerator 2.Reaction gas is from the top of regenerator 2 and by multistage cyclone separation Gas-particle separation occurs for device 3, and most of catalyst fines are caught by cyclone separator 3.The outlet of cyclone separator 3 reaction gas is direct Filter 4 is sent into, the less catalyst fines of size are caught by filled by filtration material in filter 4.The exit gas of filter 4 Into depickling reactor 5, and protective agent and beds are passed sequentially through, not only catalyst fines remaining in reaction gas are entered Row is intercepted, and realizes the selectively removing of organic acid composition in product gas.The outlet of depickling reactor 5 high-temperature gas is changed through multistage Hot device 6 reclaims heat, for preheating of oxygen-containing compound material etc., and three phase separator 8 is sent into after then cooling again through air cooler 7 Carry out the oily three phase separation of gas-liquid.Wherein isolated aqueous phase carrying device, and the compressed machine 9 of gas-phase product, gas-liquid separation Contact and redistribute again with oil-phase product after device 10, form final gas phase respectively and liquid product goes out device, wherein gas phase Product sends into olefin separation, and olefin product based on ethene and propylene is obtained through isolating and purifying.
Embodiment 1
In the present embodiment, methanol to olefins reaction uses fast fluidized bed reactor, and catalyst uses SAPO-34 molecular sieves, entered Doses is 7.5 ton hours, and reaction temperature is 470 DEG C, and reaction product feed composition is the industrial methanol of content 99.5%, using such as figure Technological process shown in 1, the mg/m of catalyst granules concentration ~ 280 of three-stage cyclone separator outlet3, the average grain of catalyst fines Footpath is 4.5 μm, and filter outlet catalyst granules concentration is ~ 40 mg/m3.Wherein, filter using glass fibre filter core as Filter part.Subsequent product gas feeding fixed bed depickling reactor(One to open one standby).Depickling react used catalyst for 10 mesh ~ The CaO of 50 mesh, protective agent and catalyst are cylinder.The actual fillings of SAPO-34 and CaO are than being 10, and deacidifying catalyst is with protecting Agent filling height is protected than being 1, catalyst granules concentration is ~ 8 mg/m in depickling reactor outlet gas3, organic acid content is less than 30 ppm.Wherein, it is 97.1% that entrained catalyst, which accumulates total removal efficiency, in product gas.Product gas is after heat exchange, air cooling to 80 DEG C, feeding three phase separator is separated, and respectively obtains gas phase, aqueous phase and oil phase.
Embodiment 2
In the present embodiment, methanol to olefins reaction uses fast fluidized bed reactor, and catalyst uses SAPO-34 molecular sieves, entered Doses is 7.5 ton hours, and reaction temperature is 470 DEG C, and reaction product feed composition is the industrial methanol of content 99.5%, using such as figure Technological process shown in 1, the mg/m of catalyst granules concentration ~ 300 of three-stage cyclone separator outlet3, the average grain of catalyst fines Footpath is 4 μm, and filter outlet catalyst granules concentration is ~ 25 mg/m3.Wherein, filter using woven wire sintered filter core as Filter element.Subsequent product gas feeding fixed bed depickling reactor(One to open one standby).It is 10 that used catalyst is reacted in depickling The Al of the mesh of mesh ~ 502O3, protective agent and catalyst are gear type.SAPO-34 and Al2O3Actual filling is than being 0.5, depickling catalysis Agent and protective agent filling height are than being that catalyst granules concentration is ~ 5 mg/m in 10, depickling reactor outlet gas3, organic acid Content is less than 25 ppm.Wherein, it is 98.3% that entrained catalyst, which accumulates total removal efficiency, in product gas.Product gas is through heat exchange, air cooling Afterwards to 65 DEG C, feeding three phase separator is separated, and respectively obtains gas phase, aqueous phase and oil phase.
Embodiment 3
In the present embodiment, methanol to olefins reaction uses fast fluidized bed reactor, and catalyst uses SAPO-34 molecular sieves, entered Doses is 7.5 ton hours, and reaction temperature is 470 DEG C, and reaction product feed composition is the industrial methanol of content 99.5%, using such as figure Technological process shown in 1, the mg/m of catalyst granules concentration ~ 200 of three-stage cyclone separator outlet3, the average grain of catalyst fines Footpath is 5.5 μm, and filter outlet catalyst granules concentration is ~ 20 mg/m3.Wherein, filter is electric precipitation formula filter.With Product gas sends into fixed bed depickling reactor afterwards(One to open one standby).It is the purpose of 10 mesh ~ 50 that used catalyst is reacted in depickling ZnO, protective agent and catalyst are trifolium-shaped.The actual fillings of SAPO-34 and ZnO are than being 6, and deacidifying catalyst is filled with protective agent Raising degree ratio is 5, and catalyst granules concentration is ~ 5 mg/m in depickling reactor outlet gas3, organic acid content is less than 15 ppm.Wherein, it is 97% that entrained catalyst, which accumulates total removal efficiency, in product gas.Product gas, to 40 DEG C, is sent into after heat exchange, air cooling Three phase separator is separated, and respectively obtains gas phase, aqueous phase and oil phase.
Embodiment 4
In the present embodiment, methanol to olefins reaction uses fast fluidized bed reactor, and catalyst uses SAPO-34 molecular sieves, entered Doses is 7.5 ton hours, and reaction temperature is 470 DEG C, and reaction product feed composition is the industrial methanol of content 99.5%, using such as figure Technological process shown in 1, the mg/m of catalyst granules concentration ~ 300 of three-stage cyclone separator outlet3, the average grain of catalyst fines Footpath is 4 μm, and filter outlet catalyst granules concentration is ~ 30 mg/m3.Wherein, filter using woven wire sintered filter core as Filter element.Subsequent product gas feeding fixed bed depickling reactor(One to open one standby).It is 10 that used catalyst is reacted in depickling The MgO of the mesh of mesh ~ 50, protective agent and catalyst are bird-nest type.The actual filling of SAPO-34 and MgO than being 2, deacidifying catalyst and Protective agent filling height is than being 0.5, and catalyst granules concentration is ~ 3 mg/m in depickling reactor outlet gas3, organic acid content Less than 10 ppm.Wherein, it is 99% that entrained catalyst, which accumulates total removal efficiency, in product gas.Product gas is after heat exchange, air cooling to 40 DEG C, feeding three phase separator is separated, and respectively obtains gas phase, aqueous phase and oil phase.
Comparative example 1
Under the conditions of as described in Example 1, pressed from both sides during three-stage cyclone separator, product gas only are set in fluidized-bed reactor outlet The total removal efficiency of band catalyst is 85%.Product gas is cooled to 190 DEG C after reclaiming heat through heat exchange, then is sequentially sent to chilling tower, water Tower is washed, reaction generation pneumatic transmission to separation of olefins unit is separated after being washed through water scrubber.Wherein, the chilling liquid of chilling bottom of towe and The cooling water at water scrubber bottom need to remove catalyst fines by liquid-solid separation filter, then be back to respectively in corresponding tower Recycle.Finite concentration NaOH solution must be continuously injected into using measuring pump in chilling tower and water scrubber, for neutralizing product gas In the organic acid composition that condenses out, but the process is whard to control.
Obviously, using the method for the present invention, the catalyst fines carried secretly in effectively less product gas solve fine powder pair The blocking problem of follow-up equipment.In addition, by setting depickling reactor, the follow-up just separating technology of optimization is stripped of in product gas Organic acid, it is to avoid corrosion of the organic acid to equipment, while add the energy regenerating path of high temperature logistics(Saving energy 20%), The investment of the equipment such as chilling tower, water-circulating pump is saved.Therefore, compared to prior art, the present invention has technically and economically Have a clear superiority.

Claims (9)

1. the preprocess method of product gas in a kind of oxygenatedchemicals olefin process, it is characterised in that comprise the following steps:
(1)The obtained high temperature hydrocarbon product gas of oxygenatedchemicals conversion first passes around cyclone separator, for initial gross separation and returns Receive catalyst fines in product;
(2)The product gas feeding filter of Cyclone outlet is thin for further separating and reclaiming catalyst in product gas Powder;
(3)The gas of filter outlet enters depickling reactor, for removing corrosive organic acid component in product gas;
(4)The exit gas of depickling reactor reclaims heat by heat exchanger, then sends into three phase separator after cooling through air cooler Gas phase, aqueous phase and oil-phase product, wherein gas-phase product feeding separation of olefins unit are obtained after condensation.
2. according to the method described in claim 1, it is characterised in that described cyclone separator is multi-cyclone, bag Include two or more cyclone separators.
3. according to the method described in claim 1, it is characterised in that described filter is selected from glass fiber filter, metal One or more in silk screen sintering candle filter, electric precipitation filter.
4. according to the method described in claim 1, it is characterised in that described heat exchanger includes heat exchanger in series or in parallel.
5. system according to claim 1, it is characterised in that described depickling reactor is fixed bed reactors, wherein Upper strata is deacidifying catalyst, and lower floor is protective agent, deacidifying catalyst and protective agent be shaped as cylinder, gear shape, cloverleaf pattern, Porous ball, cellular or bird-nest-shaped.
6. according to the method described in claim 1, it is characterised in that catalysts and deacidifying catalyst mass ratio be 0.5 ~ 10, deacidifying catalyst is with protective agent filling height than being 0.1 ~ 10.
7. according to the method described in claim 1, it is characterised in that organic in the exit gas product of described depickling reactor Sour total content is less than 30 ppm.
8. according to the method described in claim 1, it is characterised in that described three phase separator inlet temperature is 40 ~ 80 DEG C.
9. a kind of device using such as any one of claim 1-8 methods described, it is characterised in that including reactor, regenerator, Cyclone separator, filter, depickling reactor, heat exchanger, air cooler, three phase separator, compression machine, gas-liquid separator;Contain Oxygen compound is carried out in the reactor, and the catalyst inactivated after reaction regenerates in a regenerator, reaction gas from regenerator top simultaneously Occurs gas-particle separation by cyclone separator, most of catalyst fines are caught by cyclone separator, and Cyclone outlet is anti- Should gas be sent directly into filter, the less catalyst fines of size, filter are caught by filled by filtration material in filter Exit gas enters depickling reactor, and passes sequentially through protective agent and beds, depickling reactor outlet high-temperature gas warp Multi-stage heat exchanger reclaims heat, and three phase separator is sent into after then cooling again through air cooler and carries out the oily three phase separation of gas-liquid, wherein Isolated aqueous phase carrying device, and contact and lay equal stress on again with oil-phase product after the compressed machine of gas-phase product, gas-liquid separator New distribution, the gas phase and liquid product formed respectively goes out device.
CN201710580268.0A 2017-07-17 2017-07-17 The preprocess method and its device of product gas in oxygenatedchemicals olefin process Pending CN107324966A (en)

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Application publication date: 20171107