DE102007008876A1 - Method for carrying out chemical and physical processes and reaction cell - Google Patents

Abstract

The invention relates to a method and a device for carrying out chemical and physical processes, wherein for initiating these processes reactants (1, 2, 8) via pumps through in each case a Reaktandendüse (5, 6, 9) in a reaction space of a reaction cell (3) a common collision point (11) are injected and the product (4) resulting from the mixing of the reactants (1, 2, 8) is removed from the reaction space.
So that the Reaktandendüsen not clog, it is proposed that the jets of all Reaktandendüsen (5, 6, 9) are aligned at an angle α = 10 ° -170 ° to each other.

Description

The The invention relates to a method for carrying out chemical and physical Processes according to the preamble of claim 1, a reaction cell according to the preamble of claim 14 and a preferred use.

WHERE 00/61275 describes a process for carrying out chemical and physical Processes, characterized in that for initiating chemical or physical processes at least two liquid ones Media (reactants) via pumps, preferably high-pressure pumps, in each case by a Reaktandendüse in one from a reactor housing enclosed reaction space on a common collision point be sprayed that over an opening into the reaction space a gas, a vaporizing liquid, a cooling liquid or a cooling one Gas for maintaining the gas atmosphere in the reaction space, in particular in the collision point of the liquid jets, or for cooling of the resulting products, and that the resulting Products and excess gas through an outlet opening the reaction space by overpressure on the gas inlet side or by negative pressure on the product and gas outlet side are removed.

This Method has the disadvantage that in the collinear alignment two liquid jets in case of failure of a reactant, the corresponding Reaktandendüse thereby clogged that the other reactant can enter this nozzle. Another Disadvantage of the method is that very high pressures of p> 50 bar, preferably p> 500 bar and especially preferably from p = 1000-4000 be used bar. On the one hand, this means that very expensive high-pressure pumps be used. On the other hand, it also means that the entire Plant (including peripherals) designed for these high pressures and accordingly checked must become. Besides the financial disadvantages is also out of sight to prefer a process with lower pressures to work safety.

One Another disadvantage of the method described in WO 00/61275 is that the economically necessary up-scaling is not possible because with colinear alignment of the nozzles in combination with high Throughputs of the product stream from the reaction space after first exiting above, i. away from the opening from the reaction space and only later in the direction predetermined by the gas flow direction is discharged. This flow behavior leads to a broad residence time distribution or to a long residence time of the product in the reaction space. In addition, it comes to deposits of Product in the area of the gas supply, which can lead to blockages.

Generally

Of the Invention is based on the object, a method for carrying out chemical and physical processes, initiating these processes Reactants over Pumping through a Reaktandendüse in a reaction space of a Reaction cell are sprayed to a common collision point and the product resulting from the mixing of the reactants is removed from the reaction cell to improve such that the reactant nozzles do not clog.

According to the invention this Problem solved by the features of claim 1. Thereby, that the jet streams all reactant nozzles at an angle α of α = 10 ° -170 ° to each other can be aligned the reactant nozzles do not clog.

The Volume throughputs f of the reactants through the reactant nozzles are preferably in the range each f = 0.5 to 20,000 l / h, more preferably in the range of each f = 20 l / h to 5,000 l / h, more preferably in the range of each 40 l / h to 1,000 l / h, more preferably in the range of 100 each l / h to 500 l / h, so that the residence time of the product in the reaction space is minimized. l / h means liters per hour.

In According to one embodiment of the invention, the nozzle jets of the reactant nozzles are at an angle α = 30 ° -140 °, preferably α = 60 ° -110 ° to each other aligned.

Prefers are the reactants with a pressure p of p> = 1 bar, preferably p> = 10 bar, more preferably p> = 30 bar, but preferred maximum with a pressure of 49 bar in the reaction chamber of the reaction cell injected.

In an embodiment of the invention at least two reactants, each with a Reaktandendüse used.

The nozzle diameters the Reaktandendüsen at circular Reaktandendüsen are in the range of 0.1 mm-5 mm, preferably in the range of 0.5 mm-2 mm.

Special design as "reaction cell"

In a specific embodiment, the reaction cell or the reaction space has a product nozzle, through which the product is discharged from the reaction cell or its reaction space. The volume of the reaction cell closed off by the reactor housing is in the range of V = 1 μl-10 ml, preferably at V = 10 μl-3 ml. In addition, the diameter or the effective cross section the Reaktandendüsen and the pressure at which the reactants are injected, advantageously chosen so that the residence time of the product in the reaction cell or in the reaction space is shorter than 1 s (second). The effective cross-section of the product nozzle must also be adapted to this.

Specific Design as "optimized" MicroJetReactor "(MJR) In special Embodiment, the product by means of a gas, preferably compressed air, discharged from the reaction cell or from the reaction space. The Gas gets through an opening supplied and through another opening together discharged with the product.

Of the Gas flow rate f in one embodiment is f> = 500 l / h (at normal pressure), preferably at f> = 3,000 l / h (at normal pressure).

In an embodiment is for discharging the product from the reaction space compressed air with a pressure of p = 0.5-100 bar, preferably from p = 2-30 bar used.

In inventive design has the reaction cell or the reaction space, if this circular or cylindrically is formed, a diameter of d = 1 mm-50 mm, preferably d = 2mm-10 mm up.

Use of reaction cells

A reaction cell according to the invention for initiating chemical and physical processes, with at least two reactant nozzles, which the at least two reactants in the reaction space of the reaction cell, that of a housing is enclosed, splash on a common collision point, is characterized in that the jet streams of the Reaktandendüsen in one Angle α of α = 10 ° -170 ° to each other are arranged. The reactant volume flow rates are preferably in the range of 0.5 l / h-20,000 each l / h, preferably in the range of 20 l / h-5,000 l / h, particularly preferably in the range of 40 l / h-1,000 each l / h, more preferably in the range of 100 l / h to 500 l / h. The angle α is in one embodiment between α = 30 ° -140 °, preferably α = 60 ° -110 °. No way Case, the angle 0 ° or 180 °.

use the special embodiment as a "reaction cell" In special embodiment has the reaction cell is a product nozzle and the volume of the reaction cell is in the range of V = 1 μl-10 ml, preferred at V = 10 μl-3 ml. In addition is the diameter or effective cross section of the Reaktandendüsen and the pressure at which the reactants are injected, advantageous chosen so that the residence time of the product in the reaction space of the reaction cell shorter than 1 second.

use the special design as "optimized MJR" In a special embodiment is the product by means of a gas, preferably compressed air, from the Reaction cell discharged.

Of the Gas flow rate f in one embodiment is f> = 500 l / h (at normal pressure), preferably at f> = 3,000 l / h (at normal pressure).

In an embodiment is for discharging the product from the reaction space compressed air with a pressure of p = 0.5-100 bar, preferably from p = 2-30 bar used.

In inventive design has the reaction cell or the reaction space in circular or cylindrical reaction spaces a diameter of d = 1 mm-50 mm, preferably of d = 2 mm-10 mm up.

Preferred use of reaction cells

Prefers become the method according to the invention and the reaction cell according to the invention for precipitation of nanoscale particles, especially barium sulfate, under process conditions used.

The Invention thus describes a reaction cell for ultrafast Mixing of several reactants. As reactants are typically liquids z. B. Solutions or suspensions used, but it can also be gases or vaporizing liquids be used. By the ultrafast mixing of the reactants can a reaction, such as. As a precipitation, initiated. A possible Application of the reaction cell according to the invention is, as already mentioned, the precipitation of nanoscale particles under process conditions.

following the invention will be described by way of examples with accompanying figures explained in more detail.

Example 1:

In the 1a is a cross section through a 2-beam reaction cell 3 and in 1 b shows a plan view of this reaction cell according to the invention, in which two reactants 1 . 2 be reacted. The volume of the reaction cell 3 is V = 3 ml. The nozzle sizes of the circular Reaktandendüsen 5 . 6 have a diameter of d = 1.5 mm each. The volume flow rate f of the reactants used 1 . 2 is at a pressure p of p = 29 bar f = 300 l / h. The nozzle width of the product nozzle 7 is d = 4.5 mm, so that in the volume of the reaction cell or the reaction space 3 a pressure of 16 bar sets. This pressure difference causes a rapid discharge of the product 4 out the reaction cell 3 , The mean residence time in the reaction cell 3 is 5 ms.

With the reference number 10 is the housing of the reaction cell 3 and with the reference numeral 11 the collision point of the nozzle jets of the reactant nozzles 5 . 6 designated.

The reactants used are 0.3 molar aqueous barium sulphide solution and 0.3 molar, aqueous sodium sulphate solution. In the reaction cell the following reaction takes place: n Na ₂ SO ₄ + n BaS → n Na ₂ S + n BaSO ₄

The Product of the reaction is a mixture of nanoscale barium sulfate and solved Sodium sulfide in water.

Example 2:

In the 2a . 2 B is a reaction cell according to the invention 3 shown in the three reactants 1 . 2 . 8th be reacted. 2a shows a cross section and 2 B a top view of this 3-beam reaction cell 3 , The nozzle widths of the reactant nozzles 5 . 6 . 9 have a diameter of d = 0.8 mm. At product pressures of p = 17 bar, volumetric throughputs of f = 50 l / h per reactant nozzle result 5 . 6 . 9 , The volume of the reaction cell 3 is V = 450 μl, so that the mean residence time in the reaction cell 3 at t = 3 ms. The product nozzle 7 has a nozzle diameter of d = 2.4 mm, so that a pressure of p = 6 bar in the volume of the reaction cell 3 established.

As reactants, 0.5 molar, aqueous barium hydroxide solution (Ba (OH) ₂ ) and 0.5 molar aqueous sulfuric acid solution (H ₂ SO ₄ ) and a 0.01 molar aqueous solution of sodium lauryl sulfate (C ₁₂ H ₂₅ NaO ₄ S) used. In the reaction cell nanoscale barium sulfate precipitates as product, whereby the sodium lauryl sulfate goes to the surfaces of the barium sulfate particles and thus prevents further particle growth. In addition, the use of sodium lauryl sulfate leads to the hydrophobization of the barium sulfate particles.

Example 3:

In the 3 a cylindrical reaction cell according to the invention is shown, in which two reactants 1 . 2 be reacted. The product resulting from the mixing of the reactants 4 is through a gas flow 12 discharged. The nozzle widths of the reactant nozzles 5 . 6 are at d = 0.8 mm. The product pressures are at p = 45 bar, the throughputs at f = 300 l / h per Reaktandendüse 5 . 6 , The diameter of the cylindrical reaction space is d = 2.5 mm. The angle α between the reactant nozzles is α = 90 °. The gas used is compressed air at a pressure of p = 5 bar and a volume throughput of f = 6,000 l / h.

Same reference numerals in the 1a . 1b . 2a . 2 B . 3 also designate similar objects.

The reactants used are 0.5 molar aqueous barium sulphide solution and 0.5 molar aqueous zinc sulphate solution. In the reaction cell the following reaction takes place: n ZnSO ₄ + n BaS → n ZnS + n BaSO ₄

The Product of the reaction is a mixture of nanoscale zinc sulfide and nanoscale barium sulfate in water.

In the spatial representation in 4 is a reaction cell, or their reaction space or mixing chamber shown.

In the in 5 In the illustrated front view, the supply of the substances or reactants to be mixed, via two obliquely arranged feeds E and F (Reaktandendüsen), which are arranged at the angles Ma and Mb.

On the Inlet C is a gas, air supplied here. At the point where the When they come together, they become intense and mixed fast. Due to the inclination of the feeders the mixture becomes a resultant impulse in the direction of the Outlet D given, which is amplified by the air flow.

The air duct the outlet of the reaction space takes place in a nozzle-like designed channel A. The channel is shaped so that no stalling by edges or sharp cross-sectional changes occur.

One Part of the mixture already arrives in the chamber (reaction space) the wall to continue to flow there. This separation is made by the nozzle shape supported. On the walls of the mixing chamber (reaction space) can Leitkonturen B be attached, which both the flow of the mixture along the Wall as well as the air flow influence positively. The guiding contours can be ribs or grooves consist. At the exit of the feeders a collar G is attached to there premature mixing with the flowing along the wall Prevent mixture.

As in 6 shown, the feeders can be offset laterally by the dimensions Mc and Md. By this arrangement, the mixture is placed in a rotary motion, which is the mixture and improve the separation from the air.

In 7 By way of example, a flow simulation is shown which shows the mixture of the starting substances. The different shades of gray indicate the starting materials and their uniform and ideal mixture.

Preferably, a uniform and high supersaturation and a short residence time of the precipitated particles is ensured in the reaction volume. Reactants with sufficiently high concentrations are therefore advantageously used, so that under the present conditions (pH value, temperature) a supersaturation of S >> 100 (S = sulfur) is achieved. The reactants, which form a sparingly soluble precipitate under the present conditions (pH, temperature), are mixed in a small volume V, the reaction volume, the reaction volume being separated by a reactor housing or by a gas stream. If the reaction volume is limited by the reactor housing, the reaction volume is from 1 μL to 10 mL, preferably from 5 μL to 5 mL, more preferably from 10 μL to 3 mL. If the reaction volume is limited by the gas flow, the reaction volume is from 1 × 10 ^-5 μl to 100 μl, preferably from 1 × 10 ^-4 μl to 10 μl.

The inventive method is characterized by the following features that combine with each other can be:

- The jets of all Reaktandendüsen 5 . 6 . 9 are aligned at an angle α of α = 10 ° -170 ° to each other.

• – Die Reaktanden 1, 2, 8 werden mit einem Druck p von p >= 1 bar, bevorzugt p >= 10 bar, besonders bevorzugt p >= 30 bar, jedoch bevorzugt maximal mit einem Druck von 49 bar in den Reaktionsraum der Reaktionszelle 3 gespritzt.
• – Die Düsenstrahlen der Reaktandendüsen 5, 6, 9 werden in einem Winkel α von α = 30°–140°, bevorzugt α = 60°–110° zueinander ausgerichtet.
• – Es werden zwei Reaktanden 1, 2 mit jeweils einer Reaktandendüse 5, 6 verwendet.
• – Es werden drei Reaktanden 1, 2, 8 mit jeweils einer Reaktandendüse 5, 6, 9 verwendet.
• – Es werden kreisförmige oder schlitzförmige Reaktandendüsen 5, 6, 9 verwendet.
• – Die Durchmesser der kreisförmigen Reaktandendüsen 5, 6, 9 liegen im Bereich von 0,1 mm–5 mm, vorzugsweise im Bereich von 0,5 mm–2 mm.
• – Der Reaktionsraum in der Reaktionszelle 3 beinhaltet eine Produktdüse 7, über die das entstandene Produkt 4 aus dem Reaktionsraum entfernt wird.
• – Das Volumen V des Reaktionsraums liegt im Bereich von V = 1 μl–10 ml, bevorzugt bei V = 10 μl–3 ml.
• – Die Durchmesser oder der jeweilige wirksame Querschnitt der Reaktandendüsen 5, 6, 9 und der Druck, mit dem die Reaktanden 1, 2, 8 in den Reaktionsraum eingespritzt werden, werden so gewählt, dass die Verweilzeit der Reaktanden 1, 2, 8 und/oder des Produktes 4 im Reaktionsraum der Reaktionszelle 3 kürzer als 1 s (Sekunde) beträgt.
• – Das Produkt 4 wird mittels eines Gasstroms, bevorzugt Druckluft, aus dem Reaktionsraum ausgetragen.
• – Für den Gasstrom durch den Reaktionsraum wird ein Durchsatz f von f >= 500 l/h (bei Normaldruck), vorzugsweise von f >= 3.000 l/h (bei Normaldruck) verwendet.
• – Zum Austragen des Produktes 4 aus dem Reaktionsraum 3 wird Druckluft mit einem Druck von p = 0,5 bar–100 bar, vorzugsweise von p = 2 bar–30 bar verwendet.

- The volumetric throughputs of the reactants 1 . 2 . 8th through the reactant nozzles 5 . 6 . 9 are in the range of f = 20 l / h to 5000 l / h, more preferably in the range of 40 l / h to 1000 l / h, more preferably in the range of 100 l / h to 500 l / h.

• - The reactants 1 . 2 . 8th are at a pressure p of p> = 1 bar, preferably p> = 10 bar, more preferably p> = 30 bar, but preferably at a maximum pressure of 49 bar in the reaction chamber of the reaction cell 3 injected.
• - The jets of Reaktandendüsen 5 . 6 . 9 are aligned at an angle α of α = 30 ° -140 °, preferably α = 60 ° -110 ° to each other.
• - There are two reactants 1 . 2 each with a Reaktandendüse 5 . 6 used.
• - There are three reactants 1 . 2 . 8th each with a Reaktandendüse 5 . 6 . 9 used.
• - There are circular or slit-shaped Reaktandendüsen 5 . 6 . 9 used.
• - The diameters of the circular Reaktandendüsen 5 . 6 . 9 are in the range of 0.1 mm-5 mm, preferably in the range of 0.5 mm-2 mm.
• - The reaction space in the reaction cell 3 includes a product nozzle 7 about which the resulting product 4 is removed from the reaction space.
• - The volume V of the reaction space is in the range of V = 1 ul-10 ml, preferably at V = 10 ul-3 ml.
• - The diameters or the respective effective cross section of the Reaktandendüsen 5 . 6 . 9 and the pressure with which the reactants 1 . 2 . 8th are injected into the reaction space are chosen so that the residence time of the reactants 1 . 2 . 8th and / or the product 4 in the reaction space of the reaction cell 3 shorter than 1 s (second).
• - The product 4 is discharged by means of a gas stream, preferably compressed air, from the reaction space.
• For the gas flow through the reaction space, a throughput f of f> = 500 l / h (at atmospheric pressure), preferably of f> = 3,000 l / h (at normal pressure) is used.
• - To unsubscribe the product 4 from the reaction space 3 Compressed air is used at a pressure of p = 0.5 bar-100 bar, preferably of p = 2 bar-30 bar.

• – Die Düsenstrahlen der Reaktandendüsen 5, 6, 9 sind in einem Winkel α von α = 10°–170° zueinander angeordnet.
• – Der Winkel α liegt zwischen α = 30°–140°, bevorzugt α = 60°–110°.
• – Die Volumendurchsätze der Reaktanden 1, 2, 8 durch die Reaktandendüsen 5, 6, 9 liegen im Bereich von je f = 20 l/h bis 5.000 l/h, besonders bevorzugt im Bereich von je 40 l/h bis 1.000 l/h, besonders bevorzugt im Bereich von je 100 l/h bis 500 l/h.
• – Die Auslassöffnung des Reaktionsraums ist eine Produktdüse 7.
• – Die Reaktandendüsen 5, 6, 9 sind bevorzugt kreisförmig oder schlitzförmig ausgebildet.
• – Der Durchmesser kreisförmiger oder zylinderförmiger Reaktandendüsen 5, 6, 9 liegt im Bereich von 0,1–5 mm, vorzugsweise im Bereich von 0,5–2 mm.
• – Das Volumen V des Reaktionsraums in der Reaktionszelle liegt im Bereich von V = 1 μl–10 ml, bevorzugt bei V = 10 μl–3 ml.
• – Die Durchmesser oder die wirksamen Querschnitte der Reaktandendüsen 5, 6, 9 und der Druck, mit dem die Reaktanden 1, 2, 8 eingespritzt werden, sind so gewählt, dass die Verweilzeit der Reaktanden 1, 2, 8 und/oder des Produktes 4 im Reaktionsraum der Reaktionszelle 3 kürzer als 1 s ist.
• – In den Reaktionsraum mündet eine Einlassöffnung (C) zur Zuführung eines Gasstroms zur Austragung des Produktes.
• – Der Gasdurchsatz f des Gasstroms beträgt f >= 500 l/h (bei Normaldruck), vorzugsweise f >= 3.000 l/h (bei Normaldruck).
• – Der Druck p des Gasstroms liegt im Bereich von p = 0,5 bar–100 bar, vorzugsweise von p = 2 bar–30 bar.
• – Der Reaktionsraum ist zylinderförmig ausgebildet, über dessen Einlassöffnung (C) der Gasstrom zugeführt wird und dessen Auslassöffnung in die Produktdüse zum Austragen des entstandenen Produktes übergeht, wobei der wirksame Querschnitt der Einlassöffnung (C) des Reaktionsraums kleiner als der wirksame Ausgangsquerschnitt des Auslasses (D) der Produktdüse ist.
• – Die Reaktandendüsen (E, F) weisen an ihrem Austritt in den Reaktionsraum einen Kragen (G) auf, der den Querschnitt des Reaktionsraums an der Stelle des Kragens (G) verringert.
• – Die Wandungen des Reaktionsraums und/oder der Produktdüse weisen Leitkonturen (B) wie Rippen oder Nuten auf.
• – Die Austritte der Reaktandendüsen in den Reaktionsraum sind seitlich zu einer Mittelpunktsebene um die Maße M-c und M-d versetzt angeordnet, wodurch die Mischung in eine Rotationsbewegung versetzt wird.
• – Das Verfahren und die Reaktionszelle wird zur Fällung von nanoskaligen Partikeln, insbesondere Bariumsulfat, bevorzugt unter Prozessbedingungen verwendet.

The reaction cell according to the invention is characterized by the following features which can be combined with one another:

• - The jets of Reaktandendüsen 5 . 6 . 9 are arranged at an angle α of α = 10 ° -170 ° to each other.
• - The angle α is between α = 30 ° -140 °, preferably α = 60 ° -110 °.
• - The volume flow rates of the reactants 1 . 2 . 8th through the reactant nozzles 5 . 6 . 9 are in the range of f = 20 l / h to 5000 l / h, more preferably in the range of 40 l / h to 1000 l / h, more preferably in the range of 100 l / h to 500 l / h.
• The outlet opening of the reaction space is a product nozzle 7 ,
• - The reactant nozzles 5 . 6 . 9 are preferably circular or slit-shaped.
• The diameter of circular or cylindrical reactant nozzles 5 . 6 . 9 is in the range of 0.1-5 mm, preferably in the range of 0.5-2 mm.
• The volume V of the reaction space in the reaction cell is in the range of V = 1 μl-10 ml, preferably at V = 10 μl-3 ml.
• The diameters or the effective cross sections of the reactant nozzles 5 . 6 . 9 and the pressure with which the reactants 1 . 2 . 8th are chosen so that the residence time of the reactants 1 . 2 . 8th and / or the product 4 in the reaction space of the reaction cell 3 shorter than 1 s.
• - In the reaction chamber opens an inlet opening (C) for supplying a gas flow to the off carrying the product.
• - The gas flow rate f of the gas stream is f> = 500 l / h (at atmospheric pressure), preferably f> = 3,000 l / h (at atmospheric pressure).
• - The pressure p of the gas stream is in the range of p = 0.5 bar-100 bar, preferably from p = 2 bar-30 bar.
• The reaction space is cylindrical, via whose inlet opening (C) the gas stream is fed and whose outlet opening merges into the product nozzle for discharging the resulting product, the effective cross section of the inlet opening (C) of the reaction space being smaller than the effective outlet cross section of the outlet (D ) of the product nozzle is.
• - The Reaktandendüsen (E, F) have at their outlet into the reaction space on a collar (G), which reduces the cross section of the reaction space at the location of the collar (G).
• - The walls of the reaction space and / or the product nozzle have guide contours (B) such as ribs or grooves.
• The outlets of the Reaktandendüsen in the reaction chamber are arranged laterally offset to a center plane by the measures Mc and Md, whereby the mixture is set in a rotational movement.
• - The method and the reaction cell is used for the precipitation of nanoscale particles, in particular barium sulfate, preferably under process conditions.

Claims (30)

Process for carrying out chemical and physical processes, whereby reactants ( 1 . 2 . 8th ) via pumps by a respective Reaktandendüse ( 5 . 6 . 9 ) in a reaction space of a reaction cell ( 3 ) to a common collision point ( 11 ) and that by the mixing of the reactants ( 1 . 2 . 8th ) resulting product ( 4 ) is removed from the reaction space, characterized in that the jet streams of all Reaktandendüsen ( 5 . 6 . 9 ) are aligned at an angle α of α = 10 ° -170 ° to each other. Process according to Claim 1, characterized in that the volume throughputs f of the reactants ( 1 . 2 . 8th ) through the reactant nozzles ( 5 . 6 . 9 ) in the range of f = 0.5 to 20,000 l / h, preferably in the range of f = 20 l / h to 5,000 l / h, particularly preferably in the range of 40 l / h to 1,000 l / h, especially preferably in the range of 100 l / h to 500 l / h. Process according to Claim 1 or 2, characterized in that the reactants ( 1 . 2 . 8th ) with a pressure p of p> = 1 bar, preferably p> = 10 bar, more preferably p> = 30 bar, but preferably a maximum of 49 bar in the reaction space of the reaction cell ( 3 ) are sprayed. Method according to one of claims 1 to 3, characterized in that the jet streams of the reactant nozzles ( 5 . 6 . 9 ) are aligned at an angle α of α = 30 ° -140 °, preferably α = 60 ° -110 ° to each other. Method according to one of claims 1 to 4, characterized in that two reactants ( 1 . 2 ) each with a Reaktandendüse ( 5 . 6 ) be used. Method according to one of claims 1 to 4, characterized in that three reactants ( 1 . 2 . 8th ) each with a Reaktandendüse ( 5 . 6 . 9 ) be used. Method according to one of claims 1 to 6, characterized in that circular or slot-shaped Reaktandendüsen ( 5 . 6 . 9 ) be used. Process according to Claim 7, characterized in that the diameters of the circular reactant nozzles ( 5 . 6 . 9 ) in the range of 0.1 mm-5 mm, preferably in the range of 0.5 mm-2 mm. Method according to one of claims 1 to 8, characterized in that the reaction space in the reaction cell ( 3 ) a product nozzle ( 7 ) about which the resulting product ( 4 ) is removed from the reaction space. Method according to one of claims 1 to 9, characterized the volume V of the reaction space is in the range of V = 1 μl-10 ml, preferably at V = 10 .mu.l-3 ml. Method according to one of claims 1 to 10, characterized in that the diameter or the effective cross section of the Reaktandendüsen ( 5 . 6 . 9 ) and the pressure at which the reactants ( 1 . 2 . 8th ) are injected into the reaction space, are chosen so that the residence time of the reactants ( 1 . 2 . 8th ) and / or the product ( 4 ) in the reaction space of the reaction cell ( 3 ) is shorter than 1 s (second). Method according to one of claims 1 to 11, characterized in that the product ( 4 ) is discharged from the reaction space by means of a gas stream, preferably compressed air. A method according to claim 12, characterized in that for the gas flow through the reaction space, a flow rate f of f> = 500 l / h (at Nor maldruck), preferably of f> = 3000 l / h (at atmospheric pressure) is used. Method according to claim 12 or 13, characterized in that for discharging the product ( 4 ) from the reaction space ( 3 ) Compressed air at a pressure of p = 0.5 bar-100 bar, preferably of p = 2 bar-30 bar is used. Reaction cell ( 3 ) for initiating chemical and physical processes, with a reaction space in the at least two reactant nozzles ( 5 . 6 . 9 ) for the injection of the reactants ( 1 . 2 . 8th ), the reactant nozzles ( 5 . 6 . 9 ) are arranged so that the jets of reactants ( 1 . 2 . 8th ) to a common collision point ( 11 ) and with an outlet opening for discharging the resulting product ( 4 ) from the reaction space, in particular for carrying out the method according to one of claims 1 to 14, characterized in that the jet streams of the reactant nozzles ( 5 . 6 . 9 ) are arranged at an angle α of α = 10 ° - 170 ° to each other. Reaction cell according to Claim 15, characterized in that the volume throughputs of the reactants ( 1 . 2 . 8th ) through the reactant nozzles ( 5 . 6 . 9 ) in the range of f = 20 l / h to 5,000 l / h, more preferably in the range of 40 l / h to 1,000 l / h, particularly preferably in the range of 100 l / h to 500 l / h. Reaction cell according to claim 15 or 16, characterized characterized in that the angle α between α = 30 ° -140 °, preferably between α = 60 ° -110 °. Reaction cell according to one of Claims 15 to 17, characterized in that the reactant nozzles ( 5 . 6 . 9 ) are formed circular or slit-shaped. Reaction cell according to claim 18, characterized in that the diameter of circular or cylindrical reactant nozzles ( 5 . 6 . 9 ) is in the range of 0.1-5 mm, preferably in the range of 0.5-2 mm. Reaction cell according to one of claims 15 to 19, characterized in that the volume V of the reaction space in the reaction cell ( 3 ) in the range of V = 1 μl-10 ml, preferably at V = 10 μl-3 ml. Reaction cell according to one of claims 15 to 20, characterized in that the diameter or the effective cross-section of the reactant nozzles ( 5 . 6 . 9 ) and the pressure at which the reactants ( 1 . 2 . 8th ) are chosen so that the residence time of the reactants ( 1 . 2 . 8th ) and / or the product ( 4 ) in the reaction space of the reaction cell ( 3 ) is shorter than 1 s. Reaction cell according to one of claims 15 to 21, characterized in that the outlet opening is a product nozzle for discharging the product ( 4 ) from the reaction space. Reaction cell according to one of claims 15 to 22, characterized in that in the reaction space an inlet opening (C) to the feeder a gas stream discharges the product. Reaction cell according to Claim 23, characterized the gas flow rate f of the gas stream f> = 500 l / h (at atmospheric pressure), preferably f> = 3,000 l / h (at normal pressure) is. Reaction cell according to claim 23 or 24, characterized characterized in that the pressure p of the gas flow is in the range of p = 0.5 bar-100 bar, preferably from p = 2 bar-30 bar is located. Reaction cell according to one of claims 15 to 25, characterized in that the reaction space is cylindrical is over its inlet opening (C) supplied the gas stream and its outlet opening in the product nozzle for discharging the resulting product, wherein the effective Cross section of the inlet opening (C) of the reaction space is smaller than the effective starting cross-section the outlet (D) of the product nozzle is. Reaction cell according to one of claims 15 to 26, characterized in that the Reaktandendüsen (E, F) at its outlet have in the reaction space a collar (G) having the cross section of the reaction space at the location of the collar (G) is reduced. Reaction cell according to one of claims 15 to 27, characterized in that the walls of the reaction space and / or the product nozzle guide contours (B) have ribs or grooves. Reaction cell according to one of claims 15 to 28, characterized in that the outlets of the Reaktandendüsen in the Reaction space laterally to a center plane around the dimensions M-c and M-d are arranged offset, causing the mixture in a rotary motion is offset. Method according to one of claims 1 to 14 and reaction cell ( 3 ) according to one of claims 15 to 29 for the precipitation of nanoscale particles, in particular barium sulfate, preferably under process conditions.