CN1227507A - Mixing device for liquids - Google Patents
Mixing device for liquids Download PDFInfo
- Publication number
- CN1227507A CN1227507A CN97197062A CN97197062A CN1227507A CN 1227507 A CN1227507 A CN 1227507A CN 97197062 A CN97197062 A CN 97197062A CN 97197062 A CN97197062 A CN 97197062A CN 1227507 A CN1227507 A CN 1227507A
- Authority
- CN
- China
- Prior art keywords
- agitator
- housing
- mixing arrangement
- solvent
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000002156 mixing Methods 0.000 title claims abstract description 24
- 239000007788 liquid Substances 0.000 title description 12
- 239000007791 liquid phase Substances 0.000 claims abstract description 3
- 239000002904 solvent Substances 0.000 claims description 25
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 24
- 239000000203 mixture Substances 0.000 claims description 21
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 claims description 19
- 230000003647 oxidation Effects 0.000 claims description 19
- 238000007254 oxidation reaction Methods 0.000 claims description 19
- 239000002253 acid Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 11
- 238000009833 condensation Methods 0.000 claims description 10
- 230000005494 condensation Effects 0.000 claims description 10
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 9
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 9
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N diphenyl Chemical compound C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 claims description 8
- 239000000376 reactant Substances 0.000 claims description 8
- 238000010521 absorption reaction Methods 0.000 claims description 7
- 230000003197 catalytic effect Effects 0.000 claims description 7
- 239000012808 vapor phase Substances 0.000 claims description 7
- 239000012071 phase Substances 0.000 claims description 6
- 239000004305 biphenyl Substances 0.000 claims description 4
- 235000010290 biphenyl Nutrition 0.000 claims description 4
- 238000005204 segregation Methods 0.000 claims description 4
- DWNAQMUDCDVSLT-UHFFFAOYSA-N diphenyl phthalate Chemical compound C=1C=CC=C(C(=O)OC=2C=CC=CC=2)C=1C(=O)OC1=CC=CC=C1 DWNAQMUDCDVSLT-UHFFFAOYSA-N 0.000 claims description 3
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 claims description 3
- 239000003960 organic solvent Substances 0.000 claims description 3
- 239000006193 liquid solution Substances 0.000 claims 1
- 239000007789 gas Substances 0.000 description 13
- 238000002360 preparation method Methods 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- STNJBCKSHOAVAJ-UHFFFAOYSA-N Methacrolein Chemical compound CC(=C)C=O STNJBCKSHOAVAJ-UHFFFAOYSA-N 0.000 description 2
- 239000003085 diluting agent Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000000622 liquid--liquid extraction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000000638 solvent extraction Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- OFOBLEOULBTSOW-UHFFFAOYSA-N Propanedioic acid Natural products OC(=O)CC(O)=O OFOBLEOULBTSOW-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000010348 incorporation Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- VZCYOOQTPOCHFL-UPHRSURJSA-N maleic acid Chemical compound OC(=O)\C=C/C(O)=O VZCYOOQTPOCHFL-UPHRSURJSA-N 0.000 description 1
- 239000011976 maleic acid Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 239000002798 polar solvent Substances 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- VZCYOOQTPOCHFL-UHFFFAOYSA-N trans-butenedioic acid Natural products OC(=O)C=CC(O)=O VZCYOOQTPOCHFL-UHFFFAOYSA-N 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/48—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F29/00—Mixers with rotating receptacles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/05—Stirrers
- B01F27/11—Stirrers characterised by the configuration of the stirrers
- B01F27/112—Stirrers characterised by the configuration of the stirrers with arms, paddles, vanes or blades
- B01F27/1123—Stirrers characterised by the configuration of the stirrers with arms, paddles, vanes or blades sickle-shaped, i.e. curved in at least one direction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/05—Stirrers
- B01F27/11—Stirrers characterised by the configuration of the stirrers
- B01F27/19—Stirrers with two or more mixing elements mounted in sequence on the same axis
- B01F27/191—Stirrers with two or more mixing elements mounted in sequence on the same axis with similar elements
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
- B01F27/90—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms
- B01F27/902—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms cooperating with intermeshing elements fixed on the receptacle walls
- B01F27/9021—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms cooperating with intermeshing elements fixed on the receptacle walls the elements being vertically arranged, e.g. fixed on the bottom
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F2215/00—Auxiliary or complementary information in relation with mixing
- B01F2215/04—Technical information in relation with mixing
- B01F2215/0413—Numerical information
- B01F2215/0418—Geometrical information
- B01F2215/0427—Numerical distance values, e.g. separation, position
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F2215/00—Auxiliary or complementary information in relation with mixing
- B01F2215/04—Technical information in relation with mixing
- B01F2215/0413—Numerical information
- B01F2215/0418—Geometrical information
- B01F2215/0431—Numerical size values, e.g. diameter of a hole or conduit, area, volume, length, width, or ratios thereof
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Mixers Of The Rotary Stirring Type (AREA)
Abstract
Mixing device for the blending of at least two liquid phases, containing a housing (1) with an inside diameter D, in which at least one agitator (2) is equipped with two to five segment shaped blades presenting a radius of curvature K, in which the circular area inside the housing (1), covered by the rotating agitators, has a diameter E, and in which K ranges from 0.10*D to 0.30*D, preferably from 0.125*D to 0.25*D, and E ranges from 0.35*D to 0.65*D, preferably from 0.45*D to 0.55*D.
Description
The relevant a kind of mixing arrangement of the present invention and this mixing arrangement are by making the advantageous use aspect the acrylic acid to the catalytic vapor phase oxidation of propylene.
In numerous industrial process, multiple liquid must be mixed mutually.When from a kind of solution, a kind of material being made liquid-liquid extraction, must mix such as a kind of spe medium is farthest strengthened with this solution so that the quick and sufficient mass exchange that can guarantee beginning with and subsequent abundant and phase separation rapidly.For obtaining good analysing mutually, people seek a kind of mixing of appropriateness therein as possible, that is do not allow to apply too many energy when stirring.
The problem that liquid mixes for example has special importance by the catalytic vapor phase oxidation of propylene is made in the acrylic acid.In the acrylic acid process of this manufacturing, the propylene of oxidation often to mix mutually and send into gaseous oxidation then with a diluent gas or with a recycle gas that includes the unreacted educt.The reactant mixture of this gaseous oxidation is conducted to the acrylic acid of emanating in the absorbing column then.Most there acrylic acid that produced are separated out from reactant mixture with a solvent.Unabsorbed composition is removed from absorbing column with gaseous state and is transfused to a condensation stage.The condensable part of this admixture of gas is emanated out with the condensation form and is discharged from as so-called acid water.Uncondensable gaseous state part is partly re-entered gaseous oxidation and is formed so-called recycle gas.This acid water is burnt usually.In solvent, after absorption process still residual have undesirable great number deal in boil thing, for example maleic anhydride.The thing that boils in these can accumulate in the solvent under the situation of not taking corresponding measure.Can prevent that by following measure above-mentioned phenomenon from producing: in an extracting stage that adds, from solvent, extract with the thing that boils among the acid water general.
The objective of the invention is for the liquid mixture with different densities provides a kind of mixing arrangement, it can cause strengthening and mix and easy segregability.The process that another object of the present invention provides a kind of improvement is used for from a kind of aqueous solution organic solvent of emanating out.Especially, also improve by the catalytic vapor phase oxidation of propylene is made acrylic acid process.
These purposes of the present invention are to realize by a kind of mixing arrangement that is used to mix at least two kinds of liquid phases, this mixing arrangement has the housing that an internal diameter is D, at least one agitator is installed therein, this agitator has 2～5 bow-shaped leaves, and these blades have a radius of curvature K and the area of a circle turned round when it rotates for agitator in housing has a diameter E.Following condition wherein according to the present invention is applicable to that K and E:K are 0.10 * D～0.30 * D, be preferably from 0.125 * D～0.25 * D, and E is 0.35 * D～0.65 * D, is preferably 0.45 * D～0.55 * D.
One agitator preferably has 3 blades.When one by preferred agitator half of inswept diameter of the housing roughly when it rotates, during that is D=2 * E, then 1 justify and a semicircle between provide a preferable shape of blade.When using according to blender of the present invention, mass exchange and subsequent a quick thing are emanated mutually fast then to produce one in separator.Explanation to this is roughly: under the thing phase situation that is occurred, blender according to the present invention causes a kind of uniform drop size, below 1mm, causes material Transfer fast so on the one hand usually, then causes phase place segregation rapidly on the other hand.Can save the physical dimension of incorporation time and blender thus greatly.Correspondingly also can reduce the disengaging time and the physical dimension of separator.
Preferably, in the housing installed inside at least one wall is arranged, this wall has advantage ground again and is configured to vertical with housing.This flow spoiler is known and has promoted vortex effect to liquid when rotor rotation.When especially the number of the blade that just in time equals agitator and had when the number of wall and these walls are installed on the housing inboard at regular intervals, when rotating, each all forms a plurality of chambers, wherein because the motion of agitator and mixture is strengthened vortex.Yet, stoped but thus that most liquid rotates with rotor after one section rotation time.
Equally preferably a kind of mixing arrangement, wherein disposing at least two orders in housing is positioned at and has on the rotating shaft altogether and agitator that approximately have regular spaces, wherein first with last agitator in the arranged perpendicular situation next be on agitator and following agitator maintain a distance along rotating shaft and housing, this distance equals preferably to be about 0.5 times along 0.4～0.6 times of the distance of rotating shaft between two agitators.Distance between different agitators should be about equally.Can provide particularly advantageous flowing relation like this, these relations then cause required reinforcement to mix and easy segregability.
Blender can quicken not only to mix and mass exchange therefore according to the present invention owing to adopt, and segregation arranged, therefore above-mentioned mixing arrangement can be used in the process of one or more organic solvents of emanating out from a kind of aqueous solution primely, adopts the present invention therefore also greatly to improve the liquid-liquid extraction process.
According to the present invention, this new blender also can be used in by the catalytic vapor phase oxidation of propylene is made in acrylic acid development, wherein in an absorption level with one first solvent absorbing propenoic acid from the gas phase oxidation mixture, from this absorption level, first solvent and the low admixture of gas of acrylic component are taken out, and this admixture of gas preferably cooled off under 20 ℃～60 ℃ temperature in a condensation stage, the condensation of admixture of gas is taken out from this condensation stage as acid water, and the gaseous state of admixture of gas is taken out from condensation stage, and also being applied recycle gas at least in part is transported to gaseous oxidation.According to the present invention, this acid water is reached (aforesaid) mixing arrangement and is transported to a separator then together with the partial discharge at least of first solvent, so that boil in inciting somebody to action from this first solvent thing, especially maleic anhydride emanate out.First solution preferably include at least a substituted biphenyl or not substituted biphenyl, replacement or unsubstituted phenylate or diphenyl phthalate or their mixture.
Followingly the present invention is described with reference to Fig. 1～3.In the accompanying drawing
Fig. 1 illustrates a example according to mixing arrangement of the present invention with vertical view;
Fig. 2 is the example according to mixing arrangement of the present invention with two agitators;
Fig. 3 illustrates an example according to the manufacturing acrylic acid process of modification of the present invention.
Fig. 1 illustrates a blender, and it has a housing 1 and an agitator 2, and this agitator 2 can rotate around a turning cylinder R.Rotation direction is indicated with arrow in this schematic diagram.The size of agitator and configuration are corresponding to above being radius of curvature K and those conditions of being set up by the diameter E on inswept surface.Shown blade can be such as coming manufactured by dividing the method that has a pipe of suitable diameter such as one of the quartering simply.Blender shown in Figure 1 has one three blade mixer, can obtain superior especially result in practice with it.As shown in the figure, also bulkhead 3 can be housed on inner walls, to stop or to reduce the eddy flow of liquid in company with agitator.These dividing walls 3 need not to lean against fully on the housing, and they also can have a gap on housing wall, and this can cause liquid mixture is produced additional vortex effect in some cases.
Shown in Figure 2 one particularly preferred version according to blender of the present invention.The housing 21 of this blender is used for the outlet 24 of mixture for liquid to be mixed provides two inlets 22,23 and.Two agitators 27,28 are installed in housing 21 according to the above condition that is used for stirrer configuration and formation, that is their radius of curvature and by they the diameter of inswept area satisfy the condition that aforementioned front is given.Those remainders are come still disclosed parameter, that is agitator 27,28 along their common pivot axis R apart from the distance of the upside 25 of housing 21 and downside 26 by preferably as get off definite: agitator 27 is to the distance H of the upside 25 of housing 21
OWith the distance H of agitator 28 to bottom side 26
UAbout equally and equal half of the mutual distance H of two agitators.This collocation form causes particularly advantageous liquid stream condition in blender, can reach the required mixing fully with symmetrical liquid drop size so well.Also can adopt three or more agitators to substitute two agitators and dispose by this way, wherein the spacing of two adjacent agitators always is about first and last agitator or last agitator and the twice of following agitator to the distance of housing wall all the time.
Fig. 3 finally illustrates a catalytic vapor phase oxidation of having revised according to the present invention that passes through and makes acrylic acid process.Wherein propylene is sent to a reactor 33 through a pipeline 31 and such as air or the such diluent gas of water vapour through a pipeline 32, therein propylene is made catalytic vapor phase oxidation and handle, the methacrylaldehyde of Chan Shenging can be oxidized in another unshowned reactor therein.The reactant mixture of gaseous oxidation arrives a chilling apparatus 35 through a pipeline 34.Reactant mixture is cooled there and the part of absorbing medium (solvent) is evaporated, and this part medium is sent in the absorbing column 37 and therefrom through a pipeline 317 and is conducted in the chilling apparatus 35 through a cooling unit 36.The higher boiling submember of solvent is condensed in chilling apparatus 35 and takes out pipeline 319 through one and is removed.As if possible, these compositions after solvent is distillated then such as being disposed through burning.This then further is sent to from chilling apparatus 35 such as the cooling unit of being made up of cooling circuit 36 by deep cooled reactant mixture, and reactant mixture is cooled with suitable absorption temperature therein.And then reactant mixture is transmitted in the absorbing column 37.Adopt by counter-current absorption there and acrylic acid is emanated from the product of gaseous oxidation through the solvent that pipeline 317 is sent into.This ratio of solvent be as being that the mixture of the biphenyl of 75% phenylate and 25% is formed by a weight ratio, and in addition, solvent also can contain polar solvent until 25% weight ratio to be reduced such as the such solids of diphenyl phthalate and produce.Being loaded with acrylic acid solvent is admitted to cooling unit 36 and is expelled to other, not shown preparation process through a side displacer therefrom.This preparation generally includes the reextraction of a pair of low-boiling-point substance and the solvent taked in case of necessity distillation or can be compared process.The product that discharges from acrylic acid is taken out from the crown of absorbing column 37 and is sent to a chilling apparatus 38 fully, and preferably is cooled under 20 ℃～60 ℃ temperature there.The uncooled part of this product is removed through a pipeline 39, and the inert gas composition is being emanated out and be sent back to the gaseous oxidation of propylene as recycle gas through a pipeline 310 after a pipeline 311 is discharged.This recycle gas also comprises unreacted educt, nitrogen and the oxycarbide of gaseous oxidation in addition.The condensable part of the product that discharges from acrylic acid is discharged through a pipeline 312.This condensate that is referred to as acid water is made up of an aqueous solution, and this aqueous solution also comprises acetic acid, maleic acid and the formaldehyde of moderate amount and other number acid except acrylic acid.This acid water is sent to one according to mixed cell 313 of the present invention through pipeline 312 then.Acid water mixes with the part stream of first solvent there, this first solvent is introduced into and to being loaded with the preparation of acrylic acid solvent streams through pipeline 320, employing can produce a kind of to the very uniform mixing of out of phase and a kind of uniform drop size according to blender of the present invention.Mixture is imported a separator 314 after this.The thing of being emanated is discharged from this separator through pipeline 315 and 316 mutually then.Employing is according to blender of the present invention, and the time of its stirring can reduce to about 1/10, and also improved the segregation of thing phase simultaneously.The overall dimensions of blender is also corresponding to be reduced.
The acrylic acid key step of shown manufacturing can be replenished by many other steps, yet these steps but do not reduce importance of the present invention.Therefore, can carry out in many ways the preparation of from absorbing column, taking out, be loaded with acrylic acid solvent, the same acid water that produces in boil and also can stand a further preparation before or after the thing extraction.
Claims (8)
1. mixing arrangement that is used to mix at least two kinds of liquid phases, it has the housing 1 that an internal diameter is D, in housing 1, dispose at least one agitator 2, this agitator 2 has 2～5 bow-shaped leaves, this blade has radius of curvature K, wherein in housing 1, has a diameter E by agitator 2 inswept area of a circle when it rotates, it is characterized in that: the K value is 0.10 * D～0.30 * D, be preferably 0.125 * D～0.25 * D, and the E value is 0.35 * D～0.65 * D, is preferably 0.45 * D～0.55 * D.
2. mixing arrangement as claimed in claim 1 is characterized in that: agitator 2 has three bow-shaped leaves.
3. mixing arrangement as claimed in claim 1 or 2 is characterized in that: the installed inside at housing 1 has at least one wall 3, is preferably perpendicular to housing 1.
4. mixing arrangement as claimed in claim 3 is characterized in that: wall 3 is installed in the housing inboard with the spacing of rule, and the quantity of wall 3 is the same with the blade quantity that agitator 2 is had.
5. as the described mixing arrangement of one of claim 1～4, it is characterized in that: the agitator 2 that two orders are positioned at the mutual regular distance on the common rotating shaft R will be housed in housing 1, wherein first and last agitator 2 each have a distance along axle R apart from housing 1, this distance be between the single agitator 2 along 0.4～0.6 times of distance of axle R, be preferably 0.5 times.
6. according to the purposes of the described a kind of mixing arrangement of one of claim 1～5, be applied to a kind of being used for from a kind of process of one or more organic solvents of liquid solution segregation.
7. according to the purposes of the described a kind of mixing arrangement of one of claim 1～5, be applied to a kind of being used for by the catalytic vapor phase oxidation of propylene is made acrylic acid process, wherein:
With one first solvent on an absorption level from the reactant mixture of gaseous oxidation absorbing propenoic acid, from this absorption level wherein first solvent and the low admixture of gas of acrylic acid content take out,
In a condensation stage this admixture of gas is preferably cooled off under 20 ℃～60 ℃ temperature,
The condensation of admixture of gas is taken out as acid water from this condensation stage,
The gas phase of admixture of gas is taken out from this condensation stage and at least in part it is recycled to gaseous oxidation as recycle gas, and
This acid water is sent to mixing arrangement and delivers to a separator then with the part stream of this first solvent at least, so as will in boil thing, especially maleic anhydride from this first solvent, emanate.
8. purposes according to claim 7 is characterized in that: this first solvent comprises at least one biphenyl alternative or that do not substitute, a phenylate or a diphenyl phthalate that substitute or that do not substitute.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19631628A DE19631628A1 (en) | 1996-08-05 | 1996-08-05 | Mixing device for liquids |
| DE19631628.6 | 1996-08-05 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1227507A true CN1227507A (en) | 1999-09-01 |
Family
ID=7801867
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97197062A Pending CN1227507A (en) | 1996-08-05 | 1997-08-04 | Mixing device for liquids |
Country Status (10)
| Country | Link |
|---|---|
| EP (1) | EP0921851A1 (en) |
| JP (1) | JP2000515422A (en) |
| KR (1) | KR20000029819A (en) |
| CN (1) | CN1227507A (en) |
| BR (1) | BR9711014A (en) |
| CA (1) | CA2261631A1 (en) |
| DE (1) | DE19631628A1 (en) |
| ID (1) | ID17005A (en) |
| TW (1) | TW347348B (en) |
| WO (1) | WO1998005416A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107746952A (en) * | 2017-10-16 | 2018-03-02 | 包头稀土研究院 | The method for avoiding attachment crystal in mixed zone in Liquid-liquid Extraction Processes |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2798382B1 (en) | 1999-09-14 | 2001-10-26 | Atofina | PROCESS FOR THE PURIFICATION OF ACRYLIC ACID OBTAINED BY OXIDATION OF PROPYLENE AND / OR ACROLEIN |
| DE102009027401A1 (en) | 2009-07-01 | 2010-02-18 | Basf Se | Separating acrylic acid comprises cooling product gas mixture of partial gas phase oxidation of three carbon precursor compound in cooler and providing cooled product gas mixture with (non)evaporated cooling liquid into absorption column |
| DE102010001228A1 (en) | 2010-01-26 | 2011-02-17 | Basf Se | Separating acrylic acid from a product gas mixture of heterogeneously catalyzed partial gas phase oxidation of a precursor compound to acrylic acid comprises cooling product gas mixture and adding cooled mixture into absorption column |
| WO2011000808A2 (en) | 2009-07-01 | 2011-01-06 | Basf Se | Method for separating acrylic acid from the product gas mixture of a heterogeneously catalyzed partial gas phase oxidation of at least one c3-precursor compound |
| WO2019014709A1 (en) | 2017-07-17 | 2019-01-24 | Commonwealth Scientific And Industrial Research Organisation | Mixing apparatus and method of operation |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1347943A (en) * | 1972-01-12 | 1974-02-27 | Maruzen Oil Co Ltd | Process for producing fibre grade terephthalic acid |
| FR2237600A1 (en) * | 1973-07-16 | 1975-02-14 | Sfem | Motor driven food mixer-beater - has mesh disc connected to motor shaft adjacent blades to improve mixing |
| JPS54109939A (en) * | 1978-02-15 | 1979-08-29 | Mitsui Petrochem Ind Ltd | Oxidation reactor for preparing aromatic carboxylic acid |
| US5102630A (en) * | 1988-03-17 | 1992-04-07 | Amoco Corporation | Apparatus for increasing yield and product quality while reducing power costs in oxidation of an aromatic alkyl to an aromatic carboxylic acid |
| FR2638330B3 (en) * | 1988-11-03 | 1991-01-04 | Kaufler Sa | JELLY PREPARATION TANK |
-
1996
- 1996-08-05 DE DE19631628A patent/DE19631628A1/en not_active Withdrawn
-
1997
- 1997-08-04 WO PCT/EP1997/004238 patent/WO1998005416A1/en not_active Application Discontinuation
- 1997-08-04 EP EP97938872A patent/EP0921851A1/en not_active Withdrawn
- 1997-08-04 BR BR9711014A patent/BR9711014A/en not_active Application Discontinuation
- 1997-08-04 JP JP10507612A patent/JP2000515422A/en active Pending
- 1997-08-04 CA CA002261631A patent/CA2261631A1/en not_active Abandoned
- 1997-08-04 CN CN97197062A patent/CN1227507A/en active Pending
- 1997-08-04 KR KR1019997000964A patent/KR20000029819A/en not_active Application Discontinuation
- 1997-08-04 TW TW086111136A patent/TW347348B/en active
- 1997-08-05 ID IDP972712A patent/ID17005A/en unknown
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107746952A (en) * | 2017-10-16 | 2018-03-02 | 包头稀土研究院 | The method for avoiding attachment crystal in mixed zone in Liquid-liquid Extraction Processes |
Also Published As
| Publication number | Publication date |
|---|---|
| ID17005A (en) | 1997-11-27 |
| DE19631628A1 (en) | 1998-02-12 |
| CA2261631A1 (en) | 1998-02-12 |
| EP0921851A1 (en) | 1999-06-16 |
| TW347348B (en) | 1998-12-11 |
| JP2000515422A (en) | 2000-11-21 |
| WO1998005416A1 (en) | 1998-02-12 |
| BR9711014A (en) | 1999-08-17 |
| KR20000029819A (en) | 2000-05-25 |
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