DESC:FIELD
The present disclosure relates to a process and apparatus for independently processing biomass and VGO within an FCC unit.

DEFINITIONS
FCC refers to Fluid catalytic cracking which is a process for conversion of high-boiling, high-molecular weight hydrocarbon fractions of petroleum crude oils into more valuable products.
VGO refers to vacuum gas oil which is a form of oil gas, produced by vacuum distillation.
Bio fuel refers to the fuel produced from pyrolysis of biomass.
Liquid fuel refers to the fuel produced by cracking of VGO.
BACKGROUND
The background information herein below relates to the present disclosure but is not necessarily prior art.
With the diminishing supply of crude mineral oil, use of bio energy sources is becoming increasingly important for the production of liquid fuels. Biomass is viewed as a promising feedstock to obtain bio fuels.
In a conventional refinery, co-processing of biomass is done together with petroleum feedstock like vacuum gas oil (VGO), thereby producing a mixed blend of bio fuel and liquid fuel fractions. However, such mixed blends do not meet the existing fuel specifications due to the residual oxygen content requirement. The mixed blend fuel has poor stability because of the unsaturated bonds and oxygen present in the biomass. Besides, these components pose the risk of adversely affecting the materials used in automobiles.
Further, the conventional techniques of co-processing biomass and petroleum feedstock are confronted with many challenges such as increased corrosion of the riser reactor due to highly corrosive components present in biomass, and extraction of valuable chemical compounds from a blend of products of VGO and biomass processing.
There is, therefore, felt a need of alternate method for processing of biomass and VGO that mitigates the afore stated drawbacks.
OBJECTS
Some of the objects of the present disclosure, which at least one embodiment herein satisfies, are as follows.
It is an object of the present disclosure to ameliorate one or more problems of the prior art or to at least provide a useful alternative.
An object of the present disclosure is to provide a method for independently processing biomass and VGO with in a conventional FCC unit.
Another object of the present disclosure is to obtain separate streams of liquid fuel and bio fuel.
Still another object of the present disclosure is to recover the heat from the pyrolysis of biomass and utilize it for regeneration of a catalyst.
Yet another object of the present disclosure is to provide an apparatus for independently processing biomass and VGO with in a conventional FCC unit.
Other objects and advantages of the present disclosure will be more apparent from the following description, which is not intended to limit the scope of the present disclosure.
SUMMARY
The present disclosure provides a method of independently processing biomass and VGO in a fluid catalytic cracking unit to obtain separate streams of bio fuel and liquid fuel.
VGO is cracked in a riser reactor (128) in the presence of a catalyst selected from fresh catalyst and regenerated catalyst and a fluidizing medium, at a temperature in the range of 300 ºC to 800 ºC, and under a pressure in the range of 2 bar to 160 bar to obtain liquid fuel and a spent catalyst.
Biomass is pyrolyzed in a separate pyrolyzer reactor (102) in the presence of a catalyst selected from fresh catalyst, spent catalyst and regenerated catalyst and the fluidizing medium, at a temperature in the range of 350 ºC to 500 ºC, and under a pressure in the range of 1 bar to 5 bar to obtain a mixture containing bio fuel, spent catalyst and a hot residue, followed by separation to obtain separated spent catalyst and bio fuel.
The spent catalyst obtained from VGO cracking as well as biomass pyrolysis is regenerated in a regenerator (122) by utilizing the hot residue obtained from pyrolysis of biomass to obtain a regenerated catalyst and hot flue gases. The regenerated catalyst is recycled to the step of VGO cracking and/ or to both steps of VGO cracking and biomass pyrolysis.
Liquid fuel and bio-fuel can be blended together to obtain a mixed blend, wherein the amount of bio-fuel in the mixed blend is in the range of 10 to 30 wt%.
The present disclosure further provides an apparatus for independently processing biomass and VGO. The Apparatus comprises a VGO cracking unit adapted to crack VGO in presence of a catalyst selected from fresh catalyst and regenerated catalyst and a fluidizing medium to obtain liquid fuel and a spent catalyst; a biomass pyrolyzer unit adapted to pyrolyze biomass in presence of a catalyst selected from fresh catalyst, spent catalyst and regenerated catalyst and the fluidizing medium to obtain bio fuel and a hot residue; and a regenerator unit adapted to regenerate the spent catalyst from the VGO unit by utilizing heat of the hot residue from the pyrolyzer unit.
BRIEF DESCRIPTION OF THE ACCOMPANYING DRAWING
The present disclosure will now be described with the help of the accompanying drawing, in which:
Figure 1 illustrates an embodiment of an apparatus 100 for independently processing biomass and VGO with in a conventional FCC unit to obtain separate streams of liquid fuel and bio fuel.
DETAILED DESCRIPTION
Embodiments are provided so as to thoroughly and fully convey the scope of the present disclosure to the person skilled in the art. Numerous details are set forth, relating to specific components, and methods, to provide a complete understanding of embodiments of the present disclosure. It will be apparent to the person skilled in the art that the details provided in the embodiments should not be construed to limit the scope of the present disclosure. In some embodiments, well-known processes, well-known apparatus structures, and well-known techniques are not described in detail.
The terminology used, in the present disclosure, is only for the purpose of explaining a particular embodiment and such terminology shall not be considered to limit the scope of the present disclosure. As used in the present disclosure, the forms "a,” "an," and "the" may be intended to include the plural forms as well, unless the context clearly suggests otherwise. The terms "comprises," "comprising," “including,” and “having,” are open ended transitional phrases and therefore specify the presence of stated features, integers, steps, operations, elements, modules, units and/or components, but do not forbid the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof. The particular order of steps disclosed in the method and process of the present disclosure is not to be construed as necessarily requiring their performance as described or illustrated. It is also to be understood that additional or alternative steps may be employed.
The terms first, second, third, etc., should not be construed to limit the scope of the present disclosure as the aforementioned terms may be only used to distinguish one element, component, region, layer or section from another component, region, layer or section. Terms such as first, second, third etc., when used herein do not imply a specific sequence or order unless clearly suggested by the present disclosure.
The co-processing of biomass and petroleum feedstock like vacuum gas oil (VGO) in a single riser reactor to obtain a mixed blend of fuel comprising liquid fuel fractions and bio fuel is well known in the prior art. However, this mixed blend obtained by the conventional methods may not meet the existing fuel specification since they might not fulfill certain criteria such as residual oxygen requirements.
In addition, biomass pyrolysis may not require as severe conditions as those that are required for pyrolysis of petroleum feedstock. Hence, co-processing biomass with petroleum feedstock could affect the quality of the bio fuel that is obtained in the mixed blend. Further, it is difficult to separate valuable compounds obtained from pyrolysis of biomass from the mixed blend obtained from co-processing of biomass and petroleum feedstock.
The present disclosure therefore provides a method for independently processing biomass and VGO in fluid catalytic cracking unit to obtain separate streams of bio fuel and liquid fuel. The method of the present disclosure involves following steps:
a. cracking VGO in a riser reactor (128) in the presence of a catalyst selected from fresh catalyst and regenerated catalyst and a fluidizing medium to obtain a liquid fuel and a spent catalyst;
b. pyrolyzing biomass in a pyrolyzer reactor (102) in the presence of a catalyst selected from fresh catalyst, spent catalyst and regenerated catalyst and the fluidizing medium to obtain bio fuel and a hot residue;
c. regenerating the spent catalyst obtained from VGO cracking as well as biomass pyrolysis in a regenerator (122) by utilizing heat generated by the hot residue to obtain a regenerated catalyst and hot flue gases; and
d. recycling the regenerated catalyst to step (i) and/ or to both steps (i) and (ii).
The method of the present disclosure is described in detail herein below:
VGO is cracked in a riser reactor (128) in the presence of a catalyst selected from fresh catalyst and regenerated catalyst and a fluidizing medium, at a temperature in the range of 300 ºC to 800 ºC, and under a pressure in the range of 2 bar to 160 bar to obtain a first effluent comprising hydrocarbon vapors and a spent catalyst. The first effluent is introduced in a stripper (120) and stripped with steam to obtain stripped hydrocarbon vapors and the spent catalyst. The stripper (120) comprises a cyclone separator (134) to separate hydrocarbon vapors from the solid spent catalyst. The so obtained hydrocarbon vapors are condensed in a first condenser (130), followed by fractionating in a fractionator (132) to separate liquid fuel fractions and off gases.
Biomass is pyrolyzed in separate pyrolyzer reactor (102) in the presence of a catalyst selected from fresh catalyst, spent catalyst and regenerated catalyst and the fluidizing medium, at a temperature in the range of 350 ºC to 500 ºC, and under a pressure in the range of 1 bar to 5 bar to obtain a second effluent comprising pyrolysis vapors and a hot residue. The second effluent is introduced in a first separator (108) and separated to obtain pyrolysis vapors and the hot residue. The so obtained pyrolysis vapors are partially condensed in a second condenser (110), followed by separating in a second separator (112) to obtain pyrolysis vapors and condensed water. The so obtained pyrolysis vapors are further condensed in a third condenser (114), followed by fractionating in a fractionator (116) to separate bio fuel fractions and off gases.
In accordance with the embodiments of the present disclosure, the condensed water is then introduced in a heat exchanger (118) to generate steam utilizing heat from hot flue gases obtained from the regenerator (122).
In accordance with the one embodiment of the present disclosure, steam is recycled to the riser reactor (128) as a fluidizing medium.
In accordance with another embodiment of the present disclosure, steam is recycled to the pyrolyzer reactor (102) as a fluidizing medium.
In accordance with still another embodiment of the present disclosure, steam is recycled to the stripper (134) as a stripping medium.
In accordance with the embodiments of the present disclosure, the hot residue obtained from the first separator (108) is introduced in the regenerator (122) to account for the heat requirement of catalyst regeneration.
In accordance with one embodiments of the present disclosure, the FCC catalyst is E-cat.
In accordance with the embodiments of the present disclosure, the ratio of VGO to the catalyst is in the range of 1:1 to 15: 1.
In accordance with one embodiment of the present disclosure, biomass is pyrolyzed in the presence of the spent catalyst obtained from cracking of VGO. The spent catalyst is active enough to catalytically pyrolyze the solid biomass.
In accordance with the embodiments of the present disclosure, the ratio of biomass to the catalyst is in the range of 1: 1 to 1: 20. In accordance with the exemplary embodiment of the present disclosure, the ratio of biomass to the catalyst is 1: 2.
In accordance with the embodiments of the present disclosure, the fluidizing medium used is at least one selected from steam and nitrogen.
In accordance with the embodiments of the present disclosure, the biomass is at least one selected from the group consisting of wood, paper, crops, animal fats, plant oils, biological waste, algae, rice straw, coconut shell and mixtures thereof.
In accordance with the embodiments of the present disclosure, pyrolysis of biomass optionally comprises pre-treating biomass to obtain pre-treated biomass having particle size in the range of 0.2 to 1 mm and moisture content in the range of 0.1 to 10 wt%.
The present disclosure further provides an apparatus for independently processing biomass and VGO in a fluid catalytic cracking unit. The Apparatus comprises a VGO cracking unit adapted to crack VGO in the presence of a catalyst and a fluidizing medium to obtain liquid fuel and a spent catalyst. A biomass pyrolyzer unit adapted to pyrolyze biomass in presence of a catalyst and a fluidizing medium to obtain bio fuel and a spent catalyst. A regenerator unit adapted to regenerate the spent catalyst from VGO unit by utilizing heat of the hot residue obtained from the pyrolyzer unit. The Apparatus is disclosed in detail herein below:
The VGO cracking unit comprises a riser reactor (128) for cracking VGO in the presence of a catalyst selected from fresh catalyst and regenerated catalyst and a fluidizing medium to obtain a first effluent. A stripper (120) adapted to receive the first effluent from the riser reactor (128) and separate the first effluent to obtain hydrocarbon vapors and a spent catalyst. A first condenser (130) adapted to receive hydrocarbon vapors from the stripper (120) and to condense hydrocarbon vapors. A fractionator (132) adapted to receive the condensed hydrocarbon vapors from the condenser (130) and then fractionate the condensed hydrocarbon vapors into liquid fuel fractions and off gases.
In accordance with the embodiments of the present disclosure, the biomass pyrolyzing unit comprises a pyrolyzer reactor (102) adapted to pyrolyze biomass in the presence of a catalyst selected from fresh catalyst, spent catalyst and regenerated catalyst and the fluidizing medium to obtain a second effluent. A separator (108) adapted to receive the second effluent from the pyrolyzer (102) and to separate the second effluent to obtain pyrolysis vapors and the hot residue. A second condenser (110) adapted to condense pyrolysis vapors obtained from the first separator (108). A second separator (112) adapted to receive condensed pyrolysis vapors from the second condenser (110) and separate pyrolysis vapors and condensed water. A third condenser (114) adapted to receive pyrolysis vapors from the second separator (112) and further condense pyrolysis vapors. A fractionator (116) adapted to receive condensed pyrolysis vapors from the third condenser (114) and fractionate condensed pyrolysis vapors into bio fuel fractions and off gases. A heat exchanger (118) adapted to receive condensed water from the second separator (112) and generate steam utilizing heat from hot flue gases generated in the regenerator (122).
In accordance with the embodiments of the present disclosure, the biomass pyrolyzing unit comprises a hopper (104) adapted to collect biomass; and a feeder (106) adapted to provide biomass to the pyrolyzer unit (102).
In accordance with the embodiments of the present disclosure, the regenerator unit comprises a regenerator (122) adapted to receive the spent catalyst from the stripper (120) and the hot residue from the separator (108) to obtain a regenerated catalyst and hot flue gases; and a blower (124) adapted to provide air to the regenerator (122).
In accordance with the embodiments of the present disclosure, the heat exchanger (118) adapted to provide steam to the riser reactor (128).
In accordance with the embodiments of the present disclosure, the heat exchanger (118) adapted to provide steam to the stripper (120).
In accordance with the embodiments of the present disclosure, the heat exchanger (118) adapted to provide steam to the pyrolyzer reactor (102).
The present disclosure provides a method wherein separate streams of liquid fuel and bio-fuel are obtained. The method of the present disclosure facilitates easy separation of valuable products such as benzene, toluene, xylene, phenol and substituted phenols obtained from pyrolysis of biomass.
In accordance with the embodiments of the present disclosure, liquid fuel and bio-fuel can be blended together to obtain a mixed blend, wherein the amount of bio-fuel in the mixed blend is in the range of 10 to 30 wt%. The present disclosure provides a method wherein the liquid fuel and bio-fuel can be blended such that the mixed blend meets the desired fuel specification.
The method of the present disclosure utilizes the heat from hot residue obtained from pyrolysis of biomass for regeneration of the spent catalyst. Similarly, the method also utilizes the heat from hot flue gases obtained from regenerator for generation of steam. Therefore, the method of the present disclosure is energy efficient.
Further, the method of the present disclosure utilizes water obtained from pyrolysis of biomass to generate steam, which in turn is used as a fluidizing medium in cracking of VGO as well as pyrolysis of biomass. The steam is also used as a stripping medium for the effluent obtained from VGO cracking unit to separate hydrocarbon vapors and the spent catalyst.
In the method of the present disclosure, since the biomass is pyrolyzed in a separate reactor, the hardware requirements for the VGO reactor are less stringent. Biomass being corrosive in nature, requires higher hardware configuration if it is processed together with VGO, as in the case of the conventional methods.
Overall the present disclosure provides simple, economical, and energy efficient method for independently processing VGO and biomass.
The foregoing description of the embodiments has been provided for purposes of illustration and not intended to limit the scope of the present disclosure. Individual components of a particular embodiment are generally not limited to that particular embodiment, but, are interchangeable. Such variations are not to be regarded as a departure from the present disclosure, and all such modifications are considered to be within the scope of the present disclosure.
The present disclosure is further described in light of the following experiments which are set forth for illustration purpose only and not to be construed for limiting the scope of the disclosure. The following experiments can be scaled up to industrial/commercial scale and the results obtained can be extrapolated to industrial scale.
EXPERIMENTAL DETAILS
EXAMPLE 1: Pyrolysis of biomass using spent catalyst from FCC riser
Fast pyrolysis of saw dust as feed was carried out with spent catalyst, wherein the residence time was 0.2 to 10 seconds. Spent catalyst was used from the stripper after been utilized for VGO cracking in FCC riser reactor.
Pyrolysis was carried at 400 °C and atmospheric pressure. Biomass to catalyst (E-cat) ratio was 1:2, with biomass feeding rate of 300g/h.
The similar experiment was carried out using regenerated catalyst.
The product distribution obtained from both the experiments is given below in table 1.
Table 1:
Components in bio fuel With Regenerated catalyst (Wt%) With Spent Catalyst (Wt%)
Phenols and substituted phenols 32.77 29.42
Esters 11.03 2.54
Aldehydes & Ketones 5.46 8.5
Aromatics other than phenol 37.08 46.43
Acids 1.59 -
Cyclic compounds 12.15 13.1

From table 1, it is evident that the spent catalyst exhibits similar activity as the regenerated catalyst during pyrolysis of solid biomass.
TECHNICAL ADVANCES AND ECONOMICAL SIGNIFICANCE
The present disclosure described herein above has several technical advantages including, but not limited to, the realization of an apparatus and a process for independently processing biomass and VGO within separate equipment in a conventional FCC unit to obtain separate streams of liquid fuel and bio fuel, wherein the apparatus and the process:
? enables to obtain separate streams of liquid fuel and bio fuel that can be blended for obtaining the desired fuel specification;
? enables using a part of the partially spent catalyst for biomass pyrolysis;
? enables heat utilization from the pyrolysis of biomass to the catalyst stripper and regenerator unit; and
? is economical.
The embodiments herein and the various features and advantageous details thereof are explained with reference to the non-limiting embodiments in the following description. Descriptions of well-known components and processing techniques are omitted so as to not unnecessarily obscure the embodiments herein. The examples used herein are intended merely to facilitate an understanding of ways in which the embodiments herein may be practiced and to further enable those of skill in the art to practice the embodiments herein. Accordingly, the examples should not be construed as limiting the scope of the embodiments herein.
The foregoing description of the specific embodiments so fully reveal the general nature of the embodiments herein that others can, by applying current knowledge, readily modify and/or adapt for various applications such specific embodiments without departing from the generic concept, and, therefore, such adaptations and modifications should and are intended to be comprehended within the meaning and range of equivalents of the disclosed embodiments. It is to be understood that the phraseology or terminology employed herein is for the purpose of description and not of limitation. Therefore, while the embodiments herein have been described in terms of preferred embodiments, those skilled in the art will recognize that the embodiments herein can be practiced with modification within the spirit and scope of the embodiments as described herein.
The use of the expression “at least” or “at least one” suggests the use of one or more elements or ingredients or quantities, as the use may be in the embodiment of the disclosure to achieve one or more of the desired objects or results.
Any discussion of documents, acts, materials, devices, articles or the like that has been included in this specification is solely for the purpose of providing a context for the disclosure. It is not to be taken as an admission that any or all of these matters form a part of the prior art base or were common general knowledge in the field relevant to the disclosure as it existed anywhere before the priority date of this application.
The numerical values mentioned for the various physical parameters, dimensions or quantities are only approximations and it is envisaged that the values higher/lower than the numerical values assigned to the parameters, dimensions or quantities fall within the scope of the disclosure, unless there is a statement in the specification specific to the contrary.
While considerable emphasis has been placed herein on the components and component parts of the preferred embodiments, it will be appreciated that many embodiments 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 changes in the preferred embodiment as well as other embodiments of the disclosure 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.
,CLAIMS:WE CLAIM:
1. A method of independently processing biomass and VGO in a fluid catalytic cracking unit to obtain separate streams of bio fuel and liquid fuel, the method comprising:
i. cracking VGO in a VGO cracking unit in the presence of a catalyst selected from fresh catalyst and regenerated catalyst and a fluidizing medium to obtain liquid fuel and spent catalyst;
ii. pyrolyzing biomass in a pyrolyzer unit in the presence of a catalyst selected from fresh catalyst, spent catalyst and regenerated catalyst and the fluidizing medium to obtain mixture containing bio fuel, spent catalyst and hot residue;
iii. separating the spent catalyst from said mixture to obtain separated spent catalyst and bio fuel;
iv. regenerating the spent catalyst obtained in step (i) and/ or step (iii) in a regenerator by utilizing the heat from the hot residue to obtain regenerated catalyst and hot flue gases; and
v. recycling the regenerated catalyst to step (i) and/or to both steps (i) and (ii).
2. The method as claimed in claim 1, wherein step (i) of cracking VGO comprises:
a. cracking VGO in a riser reactor (128) in the presence of a catalyst selected from fresh catalyst and regenerated catalyst and a fluidizing medium, at a temperature in the range of 300 ºC to 800 ºC, and under a pressure in the range of 2 bar to 160 bar to obtain a first effluent comprising hydrocarbon vapors and spent catalyst;
b. stripping the first effluent in a stripper (120) with steam to obtain stripped hydrocarbon vapors and the spent catalyst;
c. condensing the stripped hydrocarbon vapors in a first condenser (130), followed by fractionating in a fractionator (132) to obtain liquid fuel.
3. The method as claimed in claim 1, wherein step (ii) of pyrolyzing biomass comprises:
a. pyrolyzing biomass in a pyrolyzer reactor (102) in the presence of a catalyst selected from fresh catalyst, spent catalyst and regenerated catalyst and the fluidizing medium, at a temperature in the range of 350 ºC to 500 ºC, and under a pressure in the range of 1 bar to 5 bar to obtain a second effluent comprising pyrolysis vapors and a hot residue;
b. separating the second effluent in a first separator (108) to obtain the pyrolysis vapors and the hot residue;
c. partially condensing the pyrolysis vapors in a second condenser (110), followed by separating in a second separator (112) to obtain pyrolysis vapors and condensed water;
d. condensing the pyrolysis vapors in a third condenser (114), followed by fractionating in a fractionator (116) to obtain bio-fuel.
4. The method as claimed in claim 1, wherein the ratio of VGO to the catalyst is in the range of 1:1 to 15:1.
5. The method as claimed in claim 1, biomass to the catalyst is in the range of 1: 1 to 1: 20.
6. The method as claimed in claim 1, wherein the fluidizing medium used in steps (i) and (ii) is at least one selected from steam and nitrogen.
7. The method as claimed in claim 1, wherein the biomass is at least one selected from the group consisting of wood, paper, crops, animal fats, plant oils, biological waste, algae, rice straw, coconut shell and mixtures thereof.
8. The method as claimed in claim 1, wherein the step (ii) comprises pre-treating the biomass to obtain pre-treated biomass having particle size in the range of 0.2 to 1 mm and moisture content in the range of 0.1 to 10 wt%.
9. The method as claimed in claim 3, wherein the method comprises feeding the hot residue in the regenerator (122) to generate heat for catalyst regeneration.
10. The method as claimed in claim 3, wherein the method comprises regenerating steam from the condensed water obtained in step (c) by utilizing hot flue gases generated in the regenerator (122).
11. The method as claimed in claim 11, wherein the steam is recycled to the riser reactor (128) as a fluidizing medium and/ or to the stripper (134) as a stripping medium.
12. The method as claimed in claim 1, wherein the liquid fuel and the bio-fuel are blended together to obtain a mixed blend, wherein the amount of bio-fuel in the mixed blend is in the range of 10 to 30 wt%.
13. An apparatus for independently processing biomass and VGO in a fluid catalytic cracking unit to obtain separate streams of bio fuel and liquid fuel, the apparatus comprising:
a. a VGO cracking unit adapted to crack VGO in presence of a catalyst selected from fresh catalyst and regenerated catalyst and a fluidizing medium to obtain liquid fuel and a spent catalyst;
b. a biomass pyrolyzer unit adapted to pyrolyze biomass in presence of a catalyst selected from fresh catalyst, spent catalyst and regenerated catalyst and the fluidizing medium to obtain bio fuel and a hot residue; and
c. a regenerator unit adapted to regenerate the spent catalyst from the VGO unit by utilizing heat of the hot residue from the pyrolyzer unit.
14. The apparatus as claimed in claim 13, wherein the VGO cracking unit comprises:
a. a riser reactor (128) for cracking VGO in the presence of a catalyst and a fluidizing medium to obtain a first effluent;
b. a stripper (120) adapted to receive the first effluent from the riser reactor (128) and to separate hydrocarbon vapors and a spent catalyst;
c. a first condenser (130) adapted to receive the hydrocarbon vapors from the stripper (120) and to condense the hydrocarbon vapors; and
d. a fractionator (132) adapted to receive the condensed hydrocarbon vapors from the condenser (130) and to fractionate the condensed hydrocarbon vapors into liquid fuel.
15. The apparatus as claimed in claim 13, wherein the biomass pyrolyzing unit comprises:
a. a pyrolyzer reactor (102) adapted to pyrolyze biomass in the presence of a catalyst and a fluidizing medium to obtain a second effluent;
b. a separator (108) adapted to receive the second effluent from the pyrolyzer (102) and to separate pyrolysis vapors and a hot residue;
c. a second condenser (110) adapted to receive the pyrolysis vapors from the first separator (108) and partially condense the pyrolysis vapors;
d. a second separator (112) adapted to receive the condensed pyrolysis vapors from second condenser (110) and to separate pyrolysis vapors and condensed water;
e. a third condenser (114) adapted to receive the pyrolysis vapors from the second separator (112); and
f. a fractionator (116) adapted to receive the pyrolysis vapors from the third condenser (114) and to fractionate the condensed pyrolysis vapors into bio fuel;
g. a heat exchanger (118) adapted to receive condensed water from the second separator (112) and generate steam utilizing heat from hot flue gases generated in the regenerator (122).
16. The apparatus as claimed in any one of claims 13-15, wherein the regenerator unit comprises:
a. a regenerator (122) adapted to receive the spent catalyst from the stripper (120) and the hot residue from the separator (108) to obtain regenerated catalyst and hot flue gases; and
b. a blower (124) adapted to provide air to the regenerator (122).
17. The apparatus as claimed in claim 15, wherein the heat exchanger (118) is adapted to provide steam to the riser reactor (128), the stripper (120) and the pyrolyzer reactor (102).
18. The apparatus as claimed in claim 15, wherein the biomass pyrolyzing unit comprises:
a. a hopper (104) adapted to collect biomass; and
b. a feeder (106) adapted to receive biomass from the hopper (104) and to provide the biomass to the pyrolyzer unit (102).