The present application generally relates to the field of industrial equipment. Particularly, but not exclusively, the present disclosure relates to the construction and arrangement of a reactor system. More particularly, the present disclosure discloses a multiphase reactor system with enhanced mass transfer and heat transfer.
BACKGROUND OF THE DISCLOSURE
The information in this section merely provides background information related to the present disclosure and may not constitute prior art(s).
Furfuryl alcohol is an important chemical intermediate for the production of chemical products, such as vitamin C, lysine, plasticizer, dispersing agent, lubricant, and resins. Because of the importance of furfuryl alcohol in the chemical industry and the manufacture of furfural from a renewable resource, the liquid phase furfuryl alcohol production process has attracted great research interest. In the industrial liquid phase furfuryl alcohol production process, furfuryl alcohol is produced by reacting liquid furfural with gaseous hydrogen in presence of a solid suspended catalyst in pressure ranging 30-60kg/cm2 and temperature 150-190°C. The reaction system involves all three phases' solid catalyst, liquid furfural, and gaseous hydrogen. For the mentioned reaction, hydrogen is dissolved in liquid furfural and reacts with furfural in the solid-liquid interphase of catalyst and furfural. Hence, enhancement of hydrogen mass transfer to liquid furfural has a great influence on the rate of reaction.

The reaction is significantly exothermic, and it is important to control the reaction temperature to prevent byproduct formation and/or control the product distribution. Proper temperature control of the reacting media becomes more important when the reaction is enhanced by means of enhanced mass transfer of gaseous hydrogen to liquid furfural. For removal of excess heat produced in the reaction, a reactor is fitted with an internal cooling arrangement with the provision of circulating cooling media inside the cooling tubes. Further, to initiate the reaction, it is required to increase the feed furfural temperature to the required reaction initiation temperature of 150-170°. This requirement is fulfilled by passing a heating medium, predominantly steam through the same cooling coil or through a dedicated heating coil.
To prevent the formation of byproduct and rapid runaway of reaction, a bulk quantity of liquid furfural is first taken into the reactor, and hydrogen is fed into the reactor as a limiting reactant under pressure control. For enhancing mass transfer i.e., enhanced dissolution of hydrogen in liquid furfural and heat transfer i.e., enhanced temperature control of the reactor, the reactor is fitted with an agitator system including single or multiple numbers of the impeller. Figure 1 illustrates the conventional reactor system configuration for the liquid phase semi-batch reaction system for furfuryl alcohol production from furfural. This system consists of a batch reactor (1) containing a batch of liquid furfural supplied through an inlet nozzle (4) in a batch manner and gaseous hydrogen supplied in semi-batch mode through a supply line (9). The reactor (1) consists of an agitator system (2) for mixing gas-liquid reactants and an internal heat exchange arrangement (3) for reactor heating or cooling as per requirement in the reactor (1) through supply lines (10, 11). Once the reaction is over and the product is cooled, the liquid product containing furfuryl alcohol along with slurry catalyst is transferred to the raw product tank (6) using a product pump (5) through a supply line (12). The catalyst having product liquid is circulated between the catalyst filter (8) and the product tank (6) using a filter pump (7) through supply lines (14, 15, 16). Once

sufficient catalyst removal from the reactor product is done, the filtered liquid material is transferred for further processing through a supply line (17).
In one of the prior arts, US Patent No: 5,478,535, a self-aspirator type agitator is used for enhanced mixing of gaseous phase and liquid phase. This prior art also discloses a heat exchange device for the reactor as an assembly of plates in the reactor and heat exchanging fluid flows inside those plates.
The conventional system along with the prior arts with mixing and heat transfer arrangement inside the reactor has a common problem of scale-up, as it is inevitable that the available surface area for heat transfer per unit volume (specific area) is going to reduce with increasing system volume for large system capacity. A further requirement of a larger and heavier shaft for agitator with increasing system size possess new engineering challenges. It is often a basic requirement to both heat and cool the reactor, which is done using the same heating-cooling coil in most of the cases. Dedicated heating and cooling arrangement inside the reactor many times is not possible due to space constraints. Using the same coil for heating and cooling may lead to the development of thermal stress in the coil system and is a potential source of failure. Further, operating a high-pressure hydrogen reactor fitted with an agitator shaft demands a special kind of shaft seal arrangement and is a potential source of hazard.
The present disclosure is directed to overcome one or more limitations stated above or any other limitations associated with the prior art.
OBJECTIVE OF THE DISCLOSURE
One or more drawbacks of conventional arrangements and in the prior art are overcome and additional advantages are provided through a multiphase reactor system as

described in the present disclosure. Additional features and advantages are realized through the technicalities of the present disclosure.
It is an aim of the present disclosure to provide a multiphase system with necessary and/or optional reactor heating, cooling, mixing, and filtration system for reacting one or more gaseous components with one or more liquid components in the presence or in absence of suspended fine solid or soluble catalyst in liquid in a semi-batch or continuous reactor and more specifically for the production of furfuryl alcohol by reacting furfural and hydrogen in catalyst suspended in liquid phase gas-liquid semi-batch reactor.
Another aim of the present disclosure is to provide a multiphase reactor system with enhanced mass transfer and heat transfer with no limitation to the system scale-up and enhanced process safety.
Another aim of the present disclosure is to provide a separate heating and cooling system for the reactor to eliminate the thermal stresses developed in a combined heating/cooling system.
Another aim of the present disclosure is to provide a reactor system with no rotating component like an agitator shaft, which needs a seal arrangement to prevent hydrogen leaks.
Accordingly, the present disclosure provides a multiphase reactor system with enhanced mass transfer and heat transfer with no limitation on heat exchanger design in terms of space constraints inside the reactor system.
SUMMARY OF THE DISCLOSURE

The present disclosure overcomes one or more drawbacks of conventional arrangements as described in the prior art and provides additional advantages through an arrangement as claimed in the present disclosure. Additional features and advantages are realized through the techniques of the present disclosure. Other embodiments and aspects of the disclosure are described in detail herein and are considered a part of the claimed disclosure.
In one non-limiting embodiment of the present disclosure, a multiphase reactor system to facilitate a first and second fluid reaction is disclosed. The reactor system comprises at least one multiphase reactor vessel which is configured for reacting the first fluid reactant with the second fluid reactant. A first heat exchanger is configured to receive one or more fluid reactants from the multiphase reactor vessel which heats the one or more fluid reactants to attain a reaction temperature. A second heat exchanger is configured to receive a portion of one or more fluid reactants from the multiphase reactor vessel which cools the one or more fluid reactants to maintain reaction temperature. A filter system is configured for the removal of one or more fluid reactants from a reactor product. A venturi mixing device is configured for uniform mixing of the first fluid reactant with the second fluid reactant. The multiphase reactor vessel is in fluid communication with the first heat exchanger, the second heat exchanger, and the venturi mixing device for enhanced heat and mass transfer.
In an embodiment of the present disclosure, the multiphase reactor system comprises a pump configured for increasing the pressure of one or more fluid reactants.
In an embodiment of the present disclosure, one or more fluid reactant is heated in the first heat exchanger by pressurized steam.
In an embodiment of the present disclosure, one or more fluid reactant is cooled in the second heat exchanger by cooling water.

In an embodiment of the present disclosure, the filter system is configured for the removal of a catalyst from the reactor product.
In an embodiment of the present disclosure, the venturi mixing device comprises a converging section configured for increasing velocity and reducing the pressure of the first fluid reactant. A throat area is configured for suction of the second fluid reactant due to reduced pressure of the first fluid reactant. A diverging section is configured as a pressure recovery section of the first fluid reactant and the second fluid reactant. A mesh is positioned at the end of the diverging section. A static mixer is configured for mixing the first fluid reactant with the second fluid reactant.
In an embodiment of the present disclosure, the first fluid reactant is liquid furfural, and the second fluid reactant is gaseous hydrogen.
In a non-limiting embodiment, a process of reacting a first fluid reactant with a second fluid reactant is disclosed. The process comprises steps of supplying the first fluid reactant with a catalyst through an inlet nozzle into a multiphase reactor vessel. After that circulating the first fluid reactant between the reactor and a first heat exchanger by means of a pump for heating, bypassing a venturi mixing device to attain a predetermined reaction temperature. The process further includes circulating one or more fluid reactants through bypass lines, bypassing the first heat exchanger and the venturi mixing device once the predetermined range of reaction temperature is achieved. After that supplying the second fluid reactant into the multiphase reactor for reacting the second fluid reactant with the first fluid reactant. Further, to this step, circulating a portion of the mixture of the first fluid reactant with the second fluid reactant between the reactor and the second heat exchanger for cooling if the temperature exceeds the predetermined range of reaction temperature. After that supplying a portion of the mixture of the first fluid reactant with the second fluid

reactant in the venturi mixing device for uniform mixing of the first fluid reactant with the second fluid reactant. Lastly, on completion of the reaction, the reactor product is cooled in the second heat exchanger and supplied through a filter system.
In an embodiment of the present disclosure, one or more fluid reactant is heated in the first heat exchanger by pressurized steam and is cooled in the second heat exchanger by cooling water.
In an embodiment of the present disclosure, the first fluid reactant is liquid furfural, and the second fluid reactant is gaseous hydrogen.
The foregoing summary is illustrative only and is not intended to be in any way limiting. In addition to the illustrative aspects, embodiments, and features described above, further aspects, embodiments, and features will become apparent by reference to the drawings and the following detailed description.
BRIEF DESCRIPTION OF FIGURES
The novel features and characteristics of the disclosure are set forth in the description. The disclosure itself, however, as well as a mode of use, further objectives and advantages thereof, will best be understood by reference to the following detailed description of an embodiment when read in conjunction with the accompanying drawings. One or more embodiments are now described, by way of example only, with reference to the accompanying drawings wherein like reference numerals represent like elements and in which:
Figure 1 illustrates a schematic view of a conventional reactor system configuration, according to the prior art.

Figure 2 illustrates an improved multiphase reaction system, according to an embodiment of the present disclosure.
Figure 3 illustrates a schematic diagram of a venturi mixing device, according to an embodiment of the present disclosure.
Skilled artisans will appreciate that elements in the drawings are illustrated for simplicity and have not necessarily been drawn to scale. For example, the dimensions of some of the elements in the drawings may be exaggerated relative to other elements to help to improve understanding of embodiments of the present invention.
DETAILED DESCRIPTION OF THE PRESENT DISCLOSURE
While the embodiments in the disclosure are subject to various modifications and alternative forms, specific embodiment thereof has been shown by way of example in the figures and will be described below. It should be understood, however, that it is not intended to limit the disclosure to the particular forms disclosed, but on the contrary, the present disclosure is to cover all modifications, equivalents, and alternatives falling within the scope of the disclosure.
It is to be noted that a person skilled in the art would be motivated by the present disclosure and modify various features of the system or method, without departing from the scope of the disclosure. Therefore, such modifications are considered to be part of the disclosure.
Accordingly, the drawings show only those specific details that are pertinent to understand the embodiments of the present disclosure, so as not to obscure the disclosure with details that will be readily apparent to those of ordinary skilled in the art having the benefit of the description herein. Also, a multiphase reactor system of

the present disclosure may be employed in any kind of reactor heating, cooling, mixing, and filtration system for reacting one or more gaseous components with one or more liquid components in the presence or absence of suspended fine solid or soluble catalyst in liquid in a semi-batch or continuous reactor.
The terms "comprises", "comprising", or any other variations thereof used in the disclosure, are intended to cover a non-exclusive inclusion, such that a system and method that comprises a list of components does not include only those components but may include other components not expressly listed or inherent to such system, method, or assembly, or device. In other words, one or more elements in a system or device proceeded by "comprises... a" does not, without more constraints, preclude the existence of other elements or additional elements in the system or device.
The following paragraphs describe the various components of the multiphase reactor system of the present disclosure according to an embodiment of the present description.
The present disclosure relates to a multiphase reactor system with necessary and/or optional reactor heating, cooling, mixing, and filtration system for reacting one or more gaseous components with one or more liquid components in the presence or in absence of suspended fine solid or soluble catalyst in liquid in a semi-batch or continuous reactor. In an embodiment, the reactor system is configured for the production of furfuryl alcohol by reacting furfural and hydrogen in catalyst suspended liquid phase, gas-liquid semi-batch reactor. The reactor system comprises one or more reactor vessels (21), a first heat exchanger (24) for heating, a second heat exchanger (25) for cooling, a venturi system (26) followed by a gas-liquid mixing section (51) with the help of static mixer (31) and a filter system (34) along with necessary pumps (23). In an embodiment, to improve the circulation of the liquid in the reactor vessel (21) and to prevent too fast a coalescence of the bubbles of gas in the liquid, an agitator device can be provided in the multiphase reactor system.

Accordingly, the multiphase reactor vessel (21) is configured for reacting the first fluid reactant with the second fluid reactant. The first heat exchanger (24) is configured to receive one or more fluid reactants from the multiphase reactor vessel (21) which heats one or more fluid reactants to attain a reaction temperature. The second heat exchanger (25) is configured to receive a portion of one or more fluid reactants from the multiphase reactor vessel (21) which cools the one or more fluid reactants to maintain reaction temperature. The filter system (34) is configured for removal of the one or more fluid reactants from a reactor product. The venturi mixing device (26) is configured for uniform mixing of the first fluid reactant with the second fluid reactant. The multiphase reactor vessel (21) is in fluid communication with the first heat exchanger (24), the second heat exchanger (25), and the venturi mixing device (26) for enhanced heat and mass transfer. The multiphase reactor system further comprises the pump (23) configured for increasing the pressure of one or more fluid reactants. In a preferred embodiment, the first fluid reactant is liquid furfural, and the second fluid reactant is gaseous hydrogen.
In an embodiment, an exemplary system for the production of furfural alcohol by reacting furfural and hydrogen has been illustrated in Figure 2. A predefined batch quantity of furfural with suspended fine catalyst is taken into the multiphase reactor (21) through the inlet nozzle (22). For increasing the furfural temperature to the reaction initiation temperature of 150-170°, the fluid reactant is first circulated through the first heating exchanger (24), where circulating reactor feed material is heated by a heating medium, preferably pressurized steam.
During reactor heating, the fluid reactant is circulated between the reactor (21) and the first heat exchanger (24) by means of the pump (23) and in this phase, flow is bypassed to the venturi mixing system (26). Once the desired temperature is attained, reactor material is circulated using bypass line (46), and hydrogen is supplied to the reactor

(21) through the supply line (35) under pressure control. The reactor pressure is increased and maintained at 30-60kg/cm2 by hydrogen supply. The major reaction occurring in the system is the hydrogenation of furfural to furfural alcohol:
C5H4O2 + H2^ C5H602 + Heat
The conditions at which this reaction takes place using the catalyst are 170°-190°C, at pressures no greater than 30 atmospheres. The catalyst is present in varying amounts depending upon the rate of reaction desired. The catalyst may be recycled after one batch of furfural is converted to furfuryl alcohol. In an embodiment, the catalyst may be mixed with other known catalysts useful for reducing aldehydes to alcohols.
As the reaction starts, excess heat generated in the reaction increases reactor temperature. It is important to maintain the reactor temperature between 170°-190°C for the prevention of byproduct formation, specifically the production of 2-Methyl Furan through the following reaction:
C5H602 + H2^ C5H60 + H20 + Heat
It is inadvisable to allow the reaction converting furfural into furfuryl alcohol to occur at temperatures above 200° C. Temperatures exceeding 200° C reduces the selectivity of the reaction, i.e., materials other than furfuryl alcohol will be produced in increasing quantity. For controlling the reactor temperature, a portion of the circulating fluid reactant is routed to the second heat exchanger (25) by the reactor circulation pump (23). In the second heat exchanger (25), the circulating fluid reactant is cooled by a cooling medium, preferably cooling water. During the reaction, the reactor temperature is controlled by adjusting the fraction of flow through the second heat exchanger (25) and the bypass line (46).

The mass transfer of gaseous hydrogen to liquid furfural is the key controlling factor for the rate of reaction. To enhance this mass transfer and increase the rate of reaction, which finally leads to a reduced reaction time/batch time, the venturi mixing device (26) is introduced into the system. During the reaction, a controlled portion of the liquid flow is routed through this venturi mixing device (26), which extracts the gaseous hydrogen from the reactor vapor space through a supply line (48) and mixes it with incoming liquid from the supply lines (45, 46).
The major components of the venturi mixing device (26) are illustrated in Figure 3. The circulating fluid reactant enters the venturi mixing device (26) at the converging section (27). In the converging section, fluid reactant velocity increases and pressure reduces. This reduced pressure allows suction of gaseous hydrogen from the reactor vapor space to the throat area (28) of the venturi mixing device (26) through the gas circulation line (48). The first fluid reactant and the second fluid reactant then go through a pressure recovery diverging section (29). A mesh (30) is placed at the end of the pressure recovery section and the following system with a static mixer (31) intensifies the mixing between gaseous hydrogen and liquid reactor material containing furfural. This intense mixing results in a significant increase in mass transfer and a reduction in reaction time. This gas-liquid mixed material is recycled back to the reactor (21) using the supply line (47).
On completion of the reaction hydrogen supply to the reactor (21) is closed and the fluid reactant is cooled using the second heat exchanger (25) to the desired temperature. After cooling, the fluid reactant is pumped using the reactor circulation pump (23) through the filter system (34). In an embodiment, the filter system (34) is configured for the removal of fine catalysts from the reactor product. If required, circulating the fluid reactant between the reactor (21) and the filter system (34) can be retained for a period before taking the catalyst-free product from the filter through a supply line (50).

The multiphase reactor system as disclosed in the present disclosure provides numerous advantages such as the heat transfer system being taken out of the reactor, there is no limitation to scale up, and providing a high heat transfer area for the system. Further, since the heating and cooling system is separated from the reactor vessel (21), it results in the effective design of each with a dedicated purpose and eliminates the thermal stress in a combined heating/cooling system. Further, the reactor vapor space contains no rotating component like an agitator shaft, which needs a seal arrangement to prevent hydrogen leaks. This leads to a safer system. The enhanced and uniform mixing in the venturi mixing device (26) reduces reaction time with the reduction of byproduct formation. The gas circulation and mixing device are static in nature, resulting in less maintenance and downtime. The multiphase reactor system as disclosed further provides an enhanced heat transfer with no limitation on heat exchanger design in terms of space constraint inside the reactor. This also improves the possibility of quick switching between heating to maximum cooling and thus preventing potential runaway reactions. The reaction temperature can be controlled by adjusting the circulating liquid in the exchanger and bypass. Whereas cooling water can be kept at a constant high flow rate, resulting in a more robust system of temperature control in the reactor. The reactor vessel can be used for the circulation of reactor products in the filter. An additional tank for filter circulation can be avoided. Lastly, the present disclosure of the multiphase reactor system is safer with no limitation in scale-up specifically for gas-liquid reaction in the multiphase reactor system.
While considerable emphasis has been placed herein on the particular features of this disclosure, it will be appreciated that various modifications can be made and that many changes can be made in the preferred embodiments without departing from the principles of the disclosure. These and other modifications in the nature of the disclosure or the preferred embodiments will be apparent to those skilled in the art from the disclosure herein, whereby it is to be distinctly understood that the foregoing

descriptive matter is to be interpreted merely as illustrative of the disclosure and not as a limitation.
It is to be understood that a person of ordinary skill in the art may develop a system of similar configuration without deviating from the scope of the present disclosure. Such modifications and variations may be made without departing from the scope of the present invention. Therefore, it is intended that the present disclosure covers such modifications and variations provided they come within the ambit of the appended claims and their equivalents.
Equivalents:
With respect to the use of substantially any plural and/or singular terms herein, those having skill in the art can translate from the plural to the singular and/or from the singular to the plural as is appropriate to the context and/or application. The various singular/plural permutations may be expressly set forth herein for sake of clarity.
It will be understood by those within the art that, in general, terms used herein, and especially in the appended claims (e.g., bodies of the appended claims) are generally intended as "open" terms (e.g., the term "including" should be interpreted as "including but not limited to," the term "having" should be interpreted as "having at least," the term "includes" should be interpreted as "includes but is not limited to," etc.). It will be further understood by those within the art that if a specific number of an introduced claim recitation is intended, such an intent will be explicitly recited in the claim, and in the absence of such recitation, no such intent is present. For example, as an aid to understanding, the following appended claims may contain usage of the introductory phrases "at least one" and "one or more" to introduce claim recitations. However, the use of such phrases should not be construed to imply that the introduction of a claim recitation by the indefinite articles "a" or "an" limits any particular claim containing

such introduced claim recitation to inventions containing only one such recitation, even when the same claim includes the introductory phrases "one or more" or "at least one" and indefinite articles such as "a" or "an" (e.g., "a" and/or "an" should typically be interpreted to mean "at least one" or "one or more"); the same holds true for the use of definite articles used to introduce claim recitations. In addition, even if a specific number of an introduced claim recitation is explicitly recited, those skilled in the art will recognize that such recitation should typically be interpreted to mean at least the recited number (e.g., the bare recitation of "two recitations," without other modifiers, typically means at least two recitations or two or more recitations). Furthermore, in those instances where a convention analogous to "at least one of A, B, and C, etc." is used, in general such a construction is intended in the sense one having skill in the art would understand the convention (e.g., "a system having at least one of A, B, and C" would include but not be limited to systems that have A alone, B alone, C alone, A and B together, A and C together, B and C together, and/or A, B, and C together, etc.). In those instances, where a convention analogous to "at least one of A, B, or C, etc." is used, in general, such a construction is intended in the sense one having skill in the art would understand the convention (e.g., "a system having at least one of A, B, or C" would include but not be limited to systems that have A alone, B alone, C alone, A and B together, A and C together, B and C together, and/or A, B, and C together, etc.). It will be further understood by those within the art that virtually any disjunctive word and/or phrase presenting two or more alternative terms, whether in the description, claims, or drawings, should be understood to contemplate the possibilities of including one of the terms, either of the terms or both terms. For example, the phrase "A or B" will be understood to include the possibilities of "A" or "B" or "A and B." While various aspects and embodiments have been disclosed herein, other aspects and embodiments will be apparent to those skilled in the art. The various aspects and embodiments disclosed herein are for purposes of illustration and are not intended to be limiting, with the true scope and spirit being indicated by the following claims.

List of reference numerals: -

Description Reference numerals
Prior Art
Batch reactor 1
Agitator system 2
Heat exchange arrangement 3
Inlet Nozzle 4
Product pump 5
Raw product tank 6
Filter pump 7
Catalyst filter 8
Supply lines 9-17
Present Invention
Multiphase batch reactor 21
Inlet Nozzle 22
Pump 23
First heat exchanger 24
Second heat exchanger 25
Venturi mixing device 26

Converging section 27
Throat area 28
Diverging section 29
Mesh 30
Static mixer 31
Venturi mixing device inlet 32
Venturi mixing device outlet 33
Filter system 34
Supply lines 35-50
Gas-liquid mixing section 51

We Claim:

1. A multiphase reactor system to facilitate a first and second fluid's reaction, the
reactor system comprising:
at least one multiphase reactor vessel (21) configured for reacting the first fluid reactant with the second fluid reactant;
a first heat exchanger (24) configured to receive one or more fluid reactants from the multiphase reactor vessel (21) which heats the one or more fluid reactants to attain a reaction temperature;
a second heat exchanger (25) configured to receive a portion of one or more fluid reactants from the multiphase reactor vessel (21) which cools the one or more fluid reactants to maintain reaction temperature;
a filter system (34) configured for removal of the one or more fluid reactants from a reactor product; and
a venturi mixing device (26) configured for uniform mixing of the first fluid reactant with the second fluid reactant;
wherein the multiphase reactor vessel (21) is in fluid communication with the first heat exchanger (24), the second heat exchanger (25), and the venturi mixing device (26) for enhanced heat and mass transfer.
2. The multiphase reactor system as claimed in claim 1, comprises a pump (23) configured for increasing the pressure of one or more fluid reactants.
3. The multiphase reactor system as claimed in claim 1, wherein one or more fluid reactant is heated in the first heat exchanger (24) by pressurized steam.
4. The multiphase reactor system as claimed in claim 1, wherein the one or more fluid reactant is cooled in the second heat exchanger (25) by cooling water.

5. The multiphase reactor system as claimed in claim 1, wherein the filter system (34) is configured for the removal of a catalyst from the reactor product.
6. The multiphase reactor system as claimed in claim 1, wherein the venturi mixing device (26) comprises:
a converging section (27) configured for increasing velocity and reducing the pressure of the first fluid reactant;
a throat area (28) configured for suction of second fluid reactant due to reduced pressure of the first fluid reactant;
a diverging section (29) configured as a pressure recovery section of the first fluid reactant and the second fluid reactant;
a mesh (30) positioned at the end of the diverging section (29);
a static mixer (31) configured for mixing the first fluid reactant with the second fluid reactant.
7. The multiphase reactor system as claimed in claims 1 to 6, wherein the first fluid reactant is liquid furfural, and the second fluid reactant is gaseous hydrogen.
8. A process of reacting a first fluid reactant with a second fluid reactant, the process comprising steps of:
supplying the first fluid reactant with a catalyst through an inlet nozzle (22) into a multiphase reactor vessel (21);
circulating the first fluid reactant between the reactor (21) and a first heat exchanger (24) by means of a pump (23) for heating, bypassing a venturi mixing device (26) to attain predetermined reaction temperature;

circulating the one or more fluid reactants through bypass line (46), bypassing the first heat exchanger (24) and the venturi mixing device (26) once the predetermined range of reaction temperature is achieved;
supplying the second fluid reactant into the multiphase reactor (21) for reacting the second fluid reactant with the first fluid reactant;
circulating a portion of the mixture of the first fluid reactant with the second fluid reactant between the reactor (21) and the second heat exchanger (25) for cooling if the temperature exceeds the predetermined range of reaction temperature;
supplying a portion of the mixture of the first fluid reactant with the second fluid reactant in the venturi mixing device (26) for uniform mixing of the first fluid reactant with the second fluid reactant;
wherein, on completion of the reaction, the reactor product is cooled in the second heat exchanger (25) and supplied through a filter system (34).
9. The process as claimed in claim 8, wherein the one or more fluid reactant is heated
in the first heat exchanger (24) by pressurized steam and is cooled in the second heat
exchanger (25) by cooling water.
10. The process as claimed in claim 8, wherein the first fluid reactant is liquid furfural,
and the second fluid reactant is gaseous hydrogen.