CN101352621A - Micro hydrocyclone separation and solid removal method and apparatus of MTO quench water and water of water-washing factory - Google Patents
Micro hydrocyclone separation and solid removal method and apparatus of MTO quench water and water of water-washing factory Download PDFInfo
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- CN101352621A CN101352621A CNA2008100427162A CN200810042716A CN101352621A CN 101352621 A CN101352621 A CN 101352621A CN A2008100427162 A CNA2008100427162 A CN A2008100427162A CN 200810042716 A CN200810042716 A CN 200810042716A CN 101352621 A CN101352621 A CN 101352621A
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Abstract
The invention provides a micro-vortex flow de-solid method used for MTO quenching water and washing water, comprising the steps as follows: the micro-vortex flow separation of the MTO quenching water is carried out so as to remove the contained catalyst grains wherein; the quenching purified water which is separated by micro-vortex flow is cooled so as to realize the circulation usage of water; the micro-vortex flow separation of the MTO washing water is carried out so as to remove the contained catalyst grains wherein, and the washing purified water separated by micro-vortex flow is cooled so as to realize the circulation usage of water. The invention also provides a micro-vortex flow de-solid device used for the MTO quenching water and washing water.
Description
Technical field
The invention belongs to coal transformation technology field, relate to a kind of method that adopts little cyclone separator to remove the minor amount of catalyst particles that exists in MTO technical process chilled water (chw) and the washing water, be suitable for handling the heterogeneous separation process of solid-liquid that comprises MTO technology chilled water (chw), washing water.Specifically, the invention provides a kind of MTO chilled water (chw) and washing water micro-cyclone de-solid method and device.
Background technology
MTO (methanol-to-olefins) process catalyst particle separation belongs to the physics solid-liquid and separates category, and promptly liquid takes off solid.Current traditional physics solid-liquid isolation technics mainly can be divided into: filtration, sedimentation, electrostatic separation, centrifugation, film separation etc.Recent years, membrane technology will become the later direction of giving priority to, and also belongs to the category of isolated by filtration according to the separation principle membrane separation technique along with the increase of handling fine slip.Present stage, typical separating technology has: (1) increased the concentration of its solid particle to the slip of dilute concentration according to the different in kind of processing material and the difference of isolation technics; (2) improve its stalling characteristic with preprocess method; (3) separation of solid particle; (4) take off liquid and washing.Should select the combination of different treatment process or different disposal technology according to the difference of material properties, that is, and the combination of different separation machineries and isolation technics.
The adoptable equipment of liquid denitrating catalyst particle has accurate filter, magnetic separator, ceramic membrane separator, cyclone separator etc.Preceding four kind equipments all have employing in the Separation of Solid and Liquid process, the use occasion difference, and separating effect also difference is very big.
Accurate filter exists mainly that cost is too high, maintenance cost also compares higher, and easily stop up, it is excessive to stop up the back pressure drop, and result of use is good under the little situation of low discharge, catalyst content, but under the bigger situation of big flow, catalyst content the bad problem of result of use.Also there is above problem in same ceramic membrane separator, and ceramic membrane is the main mode that adopts cross-flow filtration in catalyst separation, so generally use in the smaller device for the treatment of capacity.Magnetic separator needs to select design according to the character of catalyst own, and the liquid that contains catalyst granules is by a high gradient magnetic separator, and catalyst is subjected to very strong magnetic field force effect, is captured and holds back, and realizes the separation of catalyst.This technology application surface is narrow, and magnetic field needs to produce with electric field, and energy consumption is bigger, effect and bad under the big little content of flow.This shows that it is bigger to design and produce the difficulty that satisfies the liquid denitrating catalyst particle device production application request, that can long period stabilize the economy operation.
At oxygenate is lower carbon number hydrocarbons technology, and CN 1942558A has proposed three grades of whirlwind of elder generation, the spinning liquid method of separating and technology are handled separating of catalyst and product again.According to present international most advanced level, three grades of cyclonic separation can be removed the MTO catalyst granules more than 6 microns, and advanced cyclone can only be removed the MTO catalyst granules more than 5 microns.This separation method can effectively satisfy separating greater than 5 microns catalyst particles under the catalyst stack less unstable state states such as (three grades of whirlwind operation abnormal states of affairs) with process route.But, under nominal situation, reach 80% less than 5 microns catalyst granules content in chilling waste water, the washing water reaction waste, although catalyst granules concentration has only 50mg/L, this also can cause chilling waste water to recycle rate declining to a great extent, and the reaction water amount of getting rid of outward heightens.
In addition, although also adopt the method that one or more gas-solid separating devices are installed at the fluidized-bed reactor top in the prior art, but go out in the reaction product stream of reactor and still carry the little amount of catalyst fine particle, these catalyst particles leave quench tower with reaction waste in quench tower, cause the stripping reaction waste to contain to be difficult on a small quantity the solid particle of removing.
Therefore, contain the rerum natura of catalyst and operating condition (promptly at MTO technology chilled water (chw) and washing water, catalyst granules is evenly distributed, content is little, treating capacity is big), this area presses for develops a kind of MTO chilled water (chw) and the washing water micro-cyclone de-solid method that can remove solid particle under nominal situation.
Summary of the invention
The invention provides a kind of new MTO chilled water (chw) and washing water micro-cyclone de-solid method and device, overcome the defective that prior art exists.
On the one hand, the invention provides a kind of MTO chilled water (chw) and washing water micro-cyclone de-solid method, this method comprises:
The MTO chilled water (chw) is carried out little rotational flow separation, to remove the catalyst granules of wherein carrying secretly;
Cool off purifying waste water, to realize the recycling of water through the chilling of little rotational flow separation;
MTO washing water is carried out little rotational flow separation, to remove the catalyst granules of wherein carrying secretly; And
Water washing cleaning water through little rotational flow separation is cooled off, to realize the recycling of water.
One preferred embodiment in, the operating temperature of described MTO chilled water (chw) is 95-115 ℃, catalyst content is 100-1000mg/L, catalyst particle size is the 1-20 micron, the water-filling density of catalyst is 1300-1500kg/m
3
Another preferred embodiment in, the density of described MTO chilled water (chw) is 900-930kg/m
3, viscosity is the 0.15-0.35 centipoise.
Another preferred embodiment in, the operating temperature of described MTO washing water is 30-50 ℃, catalyst content is 70-800mg/L, catalyst particle size is the 1-10 micron.
Another preferred embodiment in, the density of described MTO washing water is 923-953kg/m
3, viscosity is the 0.551-0.751 centipoise.
Another preferred embodiment in, after having carried out described little rotational flow separation, catalyst content is reduced to below the 30mg/L.
On the other hand, the invention provides a kind of MTO chilled water (chw) and washing water micro-cyclone de fixing apparatus, this device comprises:
Be connected with quench tower, be used for the MTO chilled water (chw) is carried out little rotational flow separation, to remove little cyclone separator of the catalyst granules of wherein carrying secretly; Be connected with described little cyclone separator, be used for cooling off, to realize the recycling chilled water (chw) cooler of water purifying waste water through the chilling of little rotational flow separation; Be connected with described quench tower, be used for the olefin product that separates through quench tower is washed, further to remove the water scrubber of the catalyst granules in the olefin product; Be connected with described water scrubber, be used for MTO washing water is carried out little rotational flow separation, to remove little cyclone separator of the catalyst granules of wherein carrying secretly; And be connected with described little cyclone separator, be used for the water washing cleaning water through little rotational flow separation is cooled off, to realize the recycling washing water cooler of water.
One preferred embodiment in, described little cyclone separator is composed in parallel by single, two or more eddy flow core pipes.
Another preferred embodiment in, the entrance velocity of described little cyclone separator is that 5-10 meter per second, the pressure loss are that 0.1-0.3MPa, water inlet gauge pressure are 0.9-1.3MPa.
Another preferred embodiment in, the entrance velocity of described little cyclone separator is that 8-15 meter per second, the pressure loss are that 0.1-0.3MPa, water inlet gauge pressure are 1.2-1.6MPa.
Description of drawings
Fig. 1 is the schematic diagram according to the little rotational flow separation flow process of MTO process catalyst of one embodiment of the present invention.
Fig. 2 is the schematic diagram of the little rotational flow separation flow process of MTO process catalyst of another embodiment according to the present invention.
Fig. 3 is the schematic diagram of the little rotational flow separation flow process of MTO process catalyst of another embodiment according to the present invention.
The specific embodiment
The present inventor is through finding after the extensive and deep research, and is big for MTO chilled water (chw), this operation flux of washing water, the solid-liquid system that solids content is low, and the most effective, the most inexpensive method is to adopt cyclone separator; But because the cut diameter of conventional eddy flow, cyclone hydraulic separators is greater than 5 microns, under nominal situation, be difficult to remove the solid particle below 5 microns, therefore, invented and adopted little cyclone separation process to remove chilled water (chw) and the catalyst granules of washing in the water, the cyclone separation device applicability is extensive, simple in structure because little cyclone separator has, adaptability is strong, easy care, reliability advantages of higher, and compare with common cyclone separation device, separative efficiency is wanted high a lot (d
75Less than 3 microns).Based on above-mentioned discovery, the present invention is accomplished.
MTO is the abbreviation of Methane To Olefin, that is, and and methanol-to-olefins.The reaction mechanism of MTO is that the dehydration of methyl alcohol elder generation generates dimethyl ether, and the dehydration of the equilibrium mixture of dimethyl ether and methyl alcohol is converted into low-carbon alkene and a small amount of saturated hydrocarbons, the aromatic hydrocarbons etc. based on ethene, propylene then, has generated a large amount of water owing to dehydration in the course of reaction.Water carries little amount of catalyst with the form of steam and leaves reactor with product, and the logistics of discharging reactor is called reaction gas.For water in the separating reaction gas and olefin product, reaction gas enters quench tower and cools off.Steam transforming is that aqueous water is discharged at the bottom of by tower in quench tower, is called water at the bottom of the quench tower, and olefin product is discharged to water scrubber from cat head and washes.Through behind the quench tower, also have a small amount of short grained catalyst entrainment in the olefin product air-flow, so reaction gas enters water scrubber and further removes the catalyst solid particle.
Contain the catalyst solid particle in chilled water (chw) and the washing water, particle is big (about 1-20 micron), in order to reduce the wash number of cooling device, the service cycle of deferred mount, is necessary chilled water (chw) and washing water are carried out purified treatment.Little cyclone separator is made up of several eddy flow core pipes, and its separative efficiency is far above the cyclone of routine, and the operation pressure drop of little cyclone separator simultaneously is little, and energy consumption is low.
In a first aspect of the present invention, the little eddy flow Separation of Solid and Liquid of water purification method at the bottom of a kind of MTO technology quench tower is provided, this method comprises:
Chilled water (chw) is all discharged by the quench tower bottom, after all chilled water (chw) all passes through little cyclone separator separation, a part is to stripper, another part after the cooler cooling as chilling agent return quench tower, adopt little cyclone separator that whole chilled water (chw)s is carried out purified treatment;
Part chilled water (chw) is discharged by the quench tower bottom, after this part chilled water (chw) separates through little cyclone separator, again after cooler cooling as chilling agent return quench tower, another part chilled water (chw) is discharged the back to stripper from the middle and upper part of tower, and little cyclone separator has only carried out purified treatment to water at the bottom of the quench tower;
Part chilled water (chw) is discharged by the quench tower bottom, after this part chilled water (chw) separates through little cyclone separator, again after cooler cooling as chilling agent return quench tower, another part chilled water (chw) is divided into two parts again after discharging from the middle and upper part of tower, a part is removed stripper, another part returns quench tower to the back that cools, and little cyclone separator has only carried out purified treatment to water at the bottom of the quench tower;
Water-chilled water (chw) carries out little rotational flow separation at the bottom of adopting little cyclone separator to MTO technology quench tower, with remove catalyst granules in the chilled water (chw) (that is, and the catalyst granules of carrying secretly in the reactor, its content is about 100-1000mg/L, density is about 900-930kg/m
3, particle diameter is about the 1-20 micron); And
Water-washing water carries out little rotational flow separation at the bottom of adopting little cyclone separator to MTO technology water scrubber, with remove catalyst granules in the washing water (that is, and the catalyst granules of carrying secretly in the reactor, its content is about 70-800mg/L, density is about 923-953kg/m
3, particle diameter is about the 1-10 micron).
Preferably, the operating temperature of described chilled water (chw) is about: 95-115 ℃; The operating temperature of described washing water is about: 30-50 ℃.
Preferably, the viscosity of described chilled water (chw) is about the 0.15-0.35 centipoise; The viscosity of described washing water is about the 0.551-0.751 centipoise.
Preferably, the water-filling density of described catalyst is about 1300-1500kg/m
3
Preferably, after having carried out described little rotational flow separation, the content of catalyst can be reduced to by original 70-1000mg/L below the 30mg/L, and separation accuracy is about 2.5 microns.
In a second aspect of the present invention, a kind of MTO chilled water (chw), washing water-catalyst equipment for separating liquid from solid are provided, this device comprises:
Be connected with MTO reactor 1, be used for the resulting product of methanol to olefins reaction is carried out chilling with the air-flow that carries catalyst granules so that the quench tower 2 that the alkene of product is separated with water, most of catalyst granules enters in the water; Be connected with described quench tower 2, be used for water scrubber 3 that the olefin product after quench tower separates is washed, in order to further to remove the catalyst granules in the olefin product; Be connected with described quench tower 2, be used for chilled water (chw) is carried out the little cyclone separator 4-1 of chilled water (chw) of Separation of Solid and Liquid; Be connected with the little cyclone separator 4-1 of described chilled water (chw), be used for chilled water (chw) cooler 5-1 that the chilling that obtains through Separation of Solid and Liquid is purified waste water and cooled, in order to realize the recycling of water; Be connected with described chilled water (chw) cooler 5-1, be used for the chilling water pump 6-1 that purifies waste water and be transported to quench tower 2 through the chilling of chilled water (chw) cooler 5-1 cooling; Be connected with described water scrubber 3, be used for the washing water after washing is carried out the little cyclone separator 4-2 of washing water of rotational flow separation, in order to remove the catalyst fines in the washing water; Be connected with the little cyclone separator 4-2 of described washing water, be used for the washing water cooler 5-2 that the water washing cleaning water that obtains is cooled after separating; And be connected with described washing water cooler 5-2, the water washing cleaning water that is used for cooling off through washing water cooler 5-2 is transported to the washing water pump 6-2 of water scrubber 3, in order to realize the recycling fully of water.
Preferably, described chilled water (chw), the little cyclone separator of washing water are made up of some cover eddy flow core pipes.
Preferably, the entrance velocity of the little cyclone separator of described chilled water (chw) is about the 5-15 meter per second, and the pressure loss is about 0.1-0.3MPa, and the water inlet gauge pressure is about 0.9-1.3MPa.
Preferably, the entrance velocity of the little cyclone separator of described washing water is about the 8-15 meter per second, and the pressure loss is about 0.1-0.3MPa, and the water inlet gauge pressure is about 1.2-1.6MPa.
Preferably, the separating of trickle catalyst granules the method and apparatus of the present invention chilled water (chw) that also can be applied to MTP (preparing propylene from methanol) and OTO (producing lighter hydrocarbons) technology and the washing water from oxygenatedchemicals.
Below referring to accompanying drawing.
Fig. 1 is the schematic diagram according to the little rotational flow separation flow process of MTO process catalyst of one embodiment of the present invention.As shown in Figure 1.Methyl alcohol enters back a series of dehydration production of process under the effect of catalyst and meanwhile also generates a large amount of water based on the olefin product of ethene and propylene from MTO reactor 1 bottom; Be present in reactant in the MTO reactor 1 and the product of not consumption leaves from MTO reactor 1 top with gas form; The product and the partial reaction thing that come out from MTO reactor 1 cool off to quench tower 2, and the water that condensation is got off is discharged from the bottom of quench tower 2; A part was cooled off through chilled water (chw) cooler 5-1 after water removed catalyst granules through the little cyclone separator 4-1 of chilled water (chw) at the bottom of the quench tower; Purify waste water to carry through cooled chilling and get back to quench tower 2 by chilling water pump 6-1; A part of in addition chilling stripping of purifying waste water; Reaction gas behind the chilling is washed to water scrubber 3 subsequently, and the reaction gas that removes catalyst goes out water scrubber 3 by water scrubber 3 bottoms, and water and the catalyst fines that washes are discharged from water scrubber 3 bottoms together, are called washing water; Washing water removes catalyst by the little cyclone separator 4-2 of washing water after washing water cooler 5-2 cooling provides power to get back to water scrubber 3 circulations by washing water pump 6-2 again.
Fig. 2 is the schematic diagram of the little rotational flow separation flow process of MTO process catalyst of another embodiment according to the present invention.What this flow process was different with flow process shown in Figure 1 is, as long as part is carried out the little rotational flow separation of solid-liquid to chilled water (chw).Part chilled water (chw) is discharged from the quench tower middle and upper part, because eminence is got in the position in the tower, catalyst granules content is few more, therefore selects to extract chilled water (chw) out from tower top, and this part chilled water (chw) can directly remove stripping.
As shown in Figure 2, MTO reactor 1 internal reaction thing and product all exist with gas form, and along with the carrying out of reaction, product and a part of unreacted reactant are carried minor amount of catalyst particles together secretly and left MTO reactor 1; Cool off to quench tower 2 from the logistics that reactor 1 comes out, the water that condensation is got off is called chilled water (chw); Part chilled water (chw) is discharged from the bottom of quench tower 2, is called water at the bottom of the quench tower; Another part chilled water (chw) is discharged from the middle and upper part of quench tower 2, and the catalyst content of this part chilled water (chw) is very low, directly removes stripping; Water removes catalyst granules after over-quenching water cooler 5-1 cools off through the little cyclone separator 4-1 of chilled water (chw) at the bottom of the quench tower; Purify waste water to carry through cooled chilling and get back to quench tower 2 by chilling water pump 6-1; Reaction gas behind the chilling is washed to water scrubber 3 subsequently, and the reaction gas that removes catalyst goes out water scrubber by water scrubber 3 bottoms, and water and the catalyst fines that washes are discharged from water scrubber 3 bottoms together, are called washing water; Washing water removes catalyst by the little cyclone separator 4-2 of washing water after washing water cooler 5-2 cooling provides power to get back to water scrubber 3 circulations by washing water pump 6-2 again.
Because at quench tower endoparticle skewness, the position is high more, and it is few more to contain grain amount, so the part chilled water (chw) divides from the middle and upper part of tower and discharge, and can reduce the treating capacity of the little cyclone separator of chilled water (chw) like this, has reduced the energy consumption of separating; The catalyst granules concentration of water is compared with flow process shown in Figure 1 and is wanted high at the bottom of the quench tower simultaneously, and for solids content high processing material, little cyclone separator can reach higher separating effect.
Fig. 3 is the schematic diagram of the little rotational flow separation flow process of MTO process catalyst of another embodiment according to the present invention, and this flow process is similar to flow process shown in Figure 2, at the bottom of different the is quench tower water yield still less, more chilled water (chw) is discharged quench tower from the middle and upper part of tower.Water is delivered to the little cyclone separator of chilled water (chw) and is carried out Separation of Solid and Liquid at the bottom of the quench tower, and other chilled water (chw) part is removed stripping, and a part is used as the chilling agent to chilled water (chw) cooler cooling back.
As shown in Figure 3, the MTO reaction gas comes out the back to quench tower 2 cooling from MTO reactor 1, and the chilled water (chw) part that condensation is got off is discharged from the bottom of quench tower 2, is called water at the bottom of the quench tower; Another part chilled water (chw) is discharged from the middle and upper part of quench tower 2, and the catalyst content of this part chilled water (chw) is very low, and a part is directly removed stripping; Another part and chilled water (chw) are purified waste water to merge and are got back to quench tower 2 by chilling water pump 6-1 conveying after cool off to chilled water (chw) cooler 5-1 the back; Reaction gas behind the chilling is washed to water scrubber 3 subsequently, and the reaction gas that removes catalyst goes out water scrubber by water scrubber 3 bottoms, and water and the catalyst fines that washes are discharged from water scrubber 3 bottoms together, are called washing water; Washing water removes catalyst by the little cyclone separator 4-2 of washing water after washing water cooler 5-2 cooling provides power to get back to water scrubber 3 circulations by washing water pump 6-2 again.
Because it is few that the chilled water (chw) of discharging in the quench tower middle and upper part contains the solid particle amount, for energy efficient, the least possible chilled water (chw) is discharged at the bottom of tower.Not separated chilled water (chw) directly returns quench tower, has also played the effect of enrichment, at the bottom of the quench tower solid content of water greater than flow process shown in Figure 2, and at the bottom of the quench tower of flow process shown in Figure 2 the water solid content greater than flow process shown in Figure 1; Energy consumption but be flow process shown in Figure 1 greater than flow process shown in Figure 2, flow process shown in Figure 2 is again greater than flow process shown in Figure 3.Because the solid content height helps the efficient of rotational flow separation, therefore flow process shown in Figure 3 is optimal selection.
The pressure loss of cyclone separator is an important parameter of performance evaluation, is directly connected to the energy consumption of system.Because the particle diameter of catalyst is littler than catalyst granules in the chilled water (chw) in the washing water, for the separative efficiency that obtains, the pressure loss of the little cyclone separator of washing water is larger than the pressure loss of the little cyclone separator of chilled water (chw).
The content of water catalyst granules is about 100-1000mg/L at the bottom of the chilled water (chw) that comes out from quench tower, and density is about 1300-1500kg/m
3, particle grain size is about 1-20 μ m.(operating pressure is about 0.9-1.3MPa to contain the chilled water (chw) of little amount of catalyst, operating temperature is about 95-115 ℃) enter cyclone separator with the speed of about 5-10 meter per second, carry out liquid-solid separation in centrifugal force field, the pressure loss (pressure reduction between inlet and the treated water outlet) of regulating the little cyclone separator of chilled water (chw) is about 0.1-0.3MPa.Because the density contrast between water and the catalyst granules is very big, therefore can obtain extraordinary separating effect.Wherein, the removal efficiency of catalyst can reach more than about 80 weight %, the d of particle
75The cutting particle diameter is about below 3 microns.
The content of the washing water catalyst granules that comes out from water scrubber is about 70-800mg/L, and particle grain size is about 1-10 μ m.The chilled water (chw) (operating pressure is about 1.2-1.6MPa, and operating temperature is about 30-50 ℃) that contains little amount of catalyst enters cyclone separator with the speed of about 8-15 meter per second, carries out liquid-solid separation in centrifugal force field.Compare the large percentage that the particle of small particle diameter accounts for chilled water (chw), the pressure loss of therefore regulating the little cyclone separator of chilled water (chw) is about 0.2-0.3MPa, and the removal efficiency that wash the water catalyst this moment also can reach more than about 80 weight % the d of particle
75The cutting particle diameter is about below 3 microns.
Method and apparatus of the present invention can also be used for removing the oil droplet or the solid particle of other liquid.
The major advantage of method and apparatus of the present invention is:
The present invention adopts little cyclone separator that MTO technology chilled water (chw) and washing water have been carried out Removal of catalyst Grain is processed, and the separative efficiency height has purified water quality, reclaims the running week that catalyst granules has prolonged upstream device simultaneously Phase.
All quote in this application as a reference at all documents that the present invention mentions, just as each piece document Quoted separately as a reference such. Should be understood that in addition after having read above-mentioned instruction content of the present invention, Those skilled in the art can make various changes or modifications the present invention, and these equivalent form of values fall within this Shen equally Please the appended claims limited range.
Claims (10)
1. MTO chilled water (chw) and washing water micro-cyclone de-solid method, this method comprises:
The MTO chilled water (chw) is carried out little rotational flow separation, to remove the catalyst granules of wherein carrying secretly;
Cool off purifying waste water, to realize the recycling of water through the chilling of little rotational flow separation;
MTO washing water is carried out little rotational flow separation, to remove the catalyst granules of wherein carrying secretly; And
Water washing cleaning water through little rotational flow separation is cooled off, to realize the recycling of water.
2. the method for claim 1 is characterized in that, the operating temperature of described MTO chilled water (chw) is 95-115 ℃, and catalyst content is 100-1000mg/L, and catalyst particle size is the 1-20 micron, and the water-filling density of catalyst is 1300-1500kg/m
3
3. method as claimed in claim 1 or 2 is characterized in that, the density of described MTO chilled water (chw) is 900-930kg/m
3, viscosity is the 0.15-0.35 centipoise.
4. the method for claim 1 is characterized in that, the operating temperature of described MTO washing water is 30-50 ℃, and catalyst content is 70-800mg/L, and catalyst particle size is the 1-10 micron.
5. as claim 1 or 4 described methods, it is characterized in that the density of described MTO washing water is 923-953kg/m
3, viscosity is the 0.551-0.751 centipoise.
6. as claim 2 or 4 described methods, it is characterized in that after having carried out described little rotational flow separation, catalyst content is reduced to below the 30mg/L.
7. MTO chilled water (chw) and washing water micro-cyclone de fixing apparatus, this device comprises:
Be connected with quench tower (2), be used for the MTO chilled water (chw) is carried out little rotational flow separation, to remove little cyclone separator (4-1) of the catalyst granules of wherein carrying secretly; Be connected with described little cyclone separator (4-1), be used for cooling off, to realize the recycling chilled water (chw) cooler (5-1) of water purifying waste water through the chilling of little rotational flow separation; Be connected with described quench tower (2), be used for the olefin product that separates through quench tower (2) is washed, with the water scrubber (3) of further removing the catalyst granules in the olefin product; Be connected with described water scrubber (3), be used for MTO washing water is carried out little rotational flow separation, to remove little cyclone separator (4-2) of the catalyst granules of wherein carrying secretly; And be connected with described little cyclone separator (4-2), be used for the water washing cleaning water through little rotational flow separation is cooled off, to realize the recycling washing water cooler (5-2) of water.
8. device as claimed in claim 7 is characterized in that, described little cyclone separator is composed in parallel by single, two or more eddy flow core pipes.
9. as claim 7 or 8 described devices, it is characterized in that the entrance velocity of described little cyclone separator (4-1) is that 5-10 meter per second, the pressure loss are that 0.1-0.3MPa, water inlet gauge pressure are 0.9-1.3MPa.
10. as claim 7 or 8 described devices, it is characterized in that the entrance velocity of described little cyclone separator (4-2) is that 8-15 meter per second, the pressure loss are that 0.1-0.3MPa, water inlet gauge pressure are 1.2-1.6MPa.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100427162A CN101352621A (en) | 2008-09-10 | 2008-09-10 | Micro hydrocyclone separation and solid removal method and apparatus of MTO quench water and water of water-washing factory |
| EP09157758.5A EP2163310A3 (en) | 2008-09-10 | 2009-04-09 | Method for purifying quench water and scrubbing water from MTO (methanol-to-olefin process) by mini-hydrocyclone and apparatus used for same |
| US12/427,578 US8083951B2 (en) | 2008-09-10 | 2009-04-21 | Method for purifying quench water and scrubbing water from MTO by mini-hydrocyclone and apparatus used for same |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100427162A CN101352621A (en) | 2008-09-10 | 2008-09-10 | Micro hydrocyclone separation and solid removal method and apparatus of MTO quench water and water of water-washing factory |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102093153A (en) * | 2010-11-05 | 2011-06-15 | 华东理工大学 | Optimal combination method and device for purifying and separating MTO (Methanol To Olefins) reaction gas containing catalyst micropowder |
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| CN103951098A (en) * | 2014-04-25 | 2014-07-30 | 江苏久吾高科技股份有限公司 | Solid and oil removal method and device for chilled water and washed water in MTO (methanol to olefin) process |
| CN104030470A (en) * | 2014-06-09 | 2014-09-10 | 哈尔滨工业大学 | Raw wastewater liquid-solid temporary-separating light-heavy split double-stage rotational flow anti-blocking machine |
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| CN107382654A (en) * | 2017-09-01 | 2017-11-24 | 上海华畅环保设备发展有限公司 | Methanol-to-olefins chilled water (chw) ebullated bed separation method and device |
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2008
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| WO2012058901A1 (en) * | 2010-11-05 | 2012-05-10 | 华东理工大学 | Combined method and device for cleaning and separating mto reaction gas containing catalyst micropowders |
| CN102093153B (en) * | 2010-11-05 | 2014-04-09 | 华东理工大学 | Optimal combination method and device for purifying and separating MTO (Methanol To Olefins) reaction gas containing catalyst micropowder |
| CN102093153A (en) * | 2010-11-05 | 2011-06-15 | 华东理工大学 | Optimal combination method and device for purifying and separating MTO (Methanol To Olefins) reaction gas containing catalyst micropowder |
| CN102730857A (en) * | 2012-07-12 | 2012-10-17 | 华东理工大学 | Method and device for closed separation of washing wastewater of reaction product and surplus heat utilization in isobutene preparation by dehydrogenation of isobutane |
| CN102730857B (en) * | 2012-07-12 | 2014-07-30 | 华东理工大学 | Method and device for closed separation of washing wastewater of reaction product and surplus heat utilization in isobutene preparation by dehydrogenation of isobutane |
| CN103214333A (en) * | 2013-05-10 | 2013-07-24 | 神华集团有限责任公司 | System and process for gas-solid separation and heat exchange of alkene product prepared from organic oxygen-containing compound |
| CN103951098A (en) * | 2014-04-25 | 2014-07-30 | 江苏久吾高科技股份有限公司 | Solid and oil removal method and device for chilled water and washed water in MTO (methanol to olefin) process |
| CN103951098B (en) * | 2014-04-25 | 2015-12-30 | 江苏久吾高科技股份有限公司 | In MTO technology, quenched water and washing water take off method and the device of solid oil removing |
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| CN105330086B (en) * | 2014-06-18 | 2018-03-02 | 中国石油化工股份有限公司 | A kind of processing method of methanol-to-olefins waste water |
| CN105330086A (en) * | 2014-06-18 | 2016-02-17 | 中国石油化工股份有限公司 | Method for processing olefin waste water prepared by methanol |
| CN104826670A (en) * | 2015-04-14 | 2015-08-12 | 华东理工大学 | Method and apparatus for removing oil pollutants contained in catalyst micro-powder in MTO quenching wastewater |
| CN106643276A (en) * | 2016-12-13 | 2017-05-10 | 天津市瑞德赛恩新材料开发有限公司 | Method for solid removal of MTO quenched water and online cleaning of water scrubber |
| CN108328761A (en) * | 2017-08-29 | 2018-07-27 | 华东理工大学 | MTO washes the method and device of hydraulic art continuous operation cycle stretch-out |
| CN108328761B (en) * | 2017-08-29 | 2023-08-29 | 华东理工大学 | Method and device for prolonging continuous operation period of MTO water washing process |
| CN107382654A (en) * | 2017-09-01 | 2017-11-24 | 上海华畅环保设备发展有限公司 | Methanol-to-olefins chilled water (chw) ebullated bed separation method and device |
| CN107382654B (en) * | 2017-09-01 | 2023-08-25 | 上海华畅环保设备发展有限公司 | Separation method and device for quenching water boiling bed for preparing olefin from methanol |
| WO2022056777A1 (en) | 2020-09-17 | 2022-03-24 | 华东理工大学 | Method and apparatus for prolonging continuous operation period of methanol-to-olefins water washing process |
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