Claims:WE CLAIM:
1. A process for producing biogas from waste water organics, said process comprising the following steps:
i. pressurizing waste water containing organics at a predetermined pressure to obtain pressurized waste water;
ii. allowing said pressurized waste water to pass through a reverse osmosis unit comprising at least one reverse osmosis (RO) membrane to obtain a retentate comprising organics and a permeate comprising water;
iii. heating said retentate to obtain a heated retentate;
iv. gasifying said heated retentate in a gasification reactor to obtain a hot pressurized fluid mixture;
v. extracting the heat from said hot pressurized fluid mixture to obtain a cooled pressurized fluid mixture, and using the extracted heat in step (iii);
vi. depressurizing said cooled pressurized fluid mixture in a pressure recovery unit to obtain a depressurized pressurized fluid mixture and using the pressure recovered in step (i); and
vii. separating biogas from said depressurized fluid mixture.

2. The process as claimed in claim 1, wherein said waste water is aqueous phase obtained from hydrothermal liquefaction of biomass.

3. The process as claimed in claim 1, wherein said reverse osmosis (RO) membrane has at least one configuration selected from the group consisting of hollow fiber, spiral wound and plate tube.

4. The process as claimed in claim 1, wherein said predetermined pressure is in the range of 210 bar to 280 bar, preferably 250 bar.

5. The process as claimed in claim 1, wherein heating said retentate in step (iii) is carried out in two steps:
a) heating said retentate to a temperature in the range of 200 °C to 500 °C to obtain a first heated retentate;
b) heating said first heated retentate to a temperature in the range of 300 °C to 800 °C to obtain a second heated retentate.

6. The process as claimed in claim 5, wherein heating said retentate to obtain the first heated retentate in step (a) happens in a heat exchanger; and wherein heating said first heated retentate to obtain the second heated retentate in step (b) happens in a heater.

7. The process as claimed in claim 1, wherein said gasification in step (v) is carried out in the presence of at least one homogeneous catalyst selected from the group consisting of sodium carbonate (Na2CO3), sodium hydroxide (NaOH), potassium hydroxide (KOH) and potassium carbonate (K2CO3).

8. The process as claimed in claim 1, wherein said gasification in step (v) is optionally carried out in the presence of at least one heterogeneous catalyst comprising at least one metal selected from the group consisting of Ruthenium (Ru), Rhodium (Rh) and Nickel (Ni).

9. An apparatus (100) for producing biogas from waste water organics, said apparatus comprising:
a) a pressure pump (101) configured to pressurize waste water;
b) a reverse osmosis unit (102) comprising at least one reverse osmosis membrane, said unit (102) configured to separate:
• a retentate comprising waste water organics, and
• a permeate comprising water
from pressurized waste water;
c) a heat exchanger (104) configured to heat said retentate to obtain a first heated retentate;
d) a heater (105) configured to receive and heat said first heated retentate to obtain a second heated retentate;
e) a gasification reactor (107) configured to receive said second heated retentate and gasify said second heated retentate to obtain a hot pressurized fluid mixture,
wherein said heat exchanger (104) is configured to extract the heat of said hot pressurized fluid mixture to obtain a cooled pressurized fluid mixture;
f) a pressure recovery unit (111) configured to receive said cooled pressurized fluid mixture, and recover pressure of said cooled pressurized fluid mixture to obtain a depressurized fluid mixture;
g) a separator (113) configured to separate biogas (114) from said depressurized fluid mixture; and
h) conduits fluidly connecting said reverse osmosis unit (102), said heat exchanger (104), said heater (105), said gasification reactor (107), said pressure recovery unit (111), and said separator (113).

10. The apparatus as claimed in claim 9, which includes a hydrothermal liquefaction unit configured to provide aqueous phase of said waste water.
, Description:FIELD
The present disclosure relates to a process and an apparatus for producing biogas from waste water organics.
DEFINITION
As used in the present disclosure, the following terms are generally intended to have the meaning as set forth below, except to the extent that the context in which they are used to indicate otherwise.
Biogas: Biogas is a mixture of gases, primarily methane and carbon dioxide that is produced by the breakdown of organic matter in the absence of oxygen.
Waste water organics: Waste water organics refers to organic matter present in waste water obtained from agricultural waste, manure, municipal waste, plant material, sewage, green waste, food waste, distillery waste, marine water and various industries.
The process of reverse osmosis (RO) separates the waste water into two parts, a retentate and a permeate. Retentate refers to that part of the waste water that does not pass through the RO membrane. Permeate refers to that part of the waste water that passes through the RO membrane.
BACKGROUND
The background information herein below relates to the present disclosure but is not necessarily prior art.
The processing of waste water contaminated with organic components is essential. The waste water contains small amounts of soluble organic. The waste water organics can be converted to biofuel by hydrothermal gasification.
However, hydrothermal gasification of waste water containing small amount of waste water organics is a complex task. The hydrothermal gasification is associated with drawbacks such as high energy requirement, use of high amounts of catalyst, and need for a large process equipment due to presence of large amount of water. The above mentioned drawbacks lead to the poor process economics in terms of capital expenditure and operating cost.
There is, therefore, felt a need for the process and an apparatus that can effectively convert the waste water organics to biogas.
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.
Another object of the present disclosure is to provide a process for producing biogas from waste water organics.
Yet another object of the present disclosure is to provide an apparatus for producing biogas from waste water organics.
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
In accordance with an aspect of the present disclosure, there is provided an apparatus for producing biogas from waste water organics.
The apparatus of the present disclosure comprises a reverse osmosis unit comprising at least one reverse osmosis membrane, configured for receiving pressurized waste water containing organics and allowing water to pass therethrough to obtain a retentate comprising organics and a permeate comprising water. A pressure pump for pressurizing and forcing the waste water to the reverse osmosis unit. A heat exchanger configured for receiving and heating the retentate to obtain a first heated retentate. A first conduit for transferring the retentate to the heat exchanger. A heater configured for receiving and heating the first heated retentate to obtain a second heated retentate. A second conduit for transferring the first heated retentate to the heater. A gasification reactor configured for receiving the second heated retentate and gasifying the second heated retentate to obtain a hot pressurized fluid mixture. The hot pressurized fluid mixture is passed in the heat exchanger to recover the heat of the hot pressurized fluid mixture for heating the retentate to obtain the first heated retentate and to obtain a cooled pressurized fluid mixture. A third conduit for transferring the second heated retentate to the gasification reactor. A fourth conduit for transferring the hot pressurized fluid mixture to the heat exchanger. A recovery unit configured for receiving the cooled pressurized fluid mixture and recovering pressure of the cooled pressurized fluid mixture to obtain a depressurized fluid mixture. A fifth conduit for transferring a cooled pressurized fluid mixture to the pressure recovery unit. A separator for separating biogas and treated water from the depressurized fluid mixture. A sixth conduit for transferring the depressurized fluid mixture to the separator.
In accordance with another aspect of the present disclosure, there is provided a process for producing biogas from waste water organics.
The process comprises pressurizing waste water containing organics at a predetermined pressure to obtain pressurized waste water. The pressurized waste water is transferred through a reverse osmosis (RO) unit comprising at least one reverse osmosis (RO) membrane to obtain retentate comprising organics, and permeate comprising water. In the next step, the retentate is heated to obtain a heated retentate. The permeate can be recycled.
In accordance with one embodiment of the present disclosure, heating the retentate is carried out in two steps:
a) heating the retentate to a temperature in the range of 200 °C to 500 °C to obtain a first heated retentate;
b) heating the first heated retentate to a temperature in the range of 300 °C to 800 °C to obtain a second heated retentate.
The retentate is heated in a heat exchanger to obtain a first heated retentate and the first heated retentate is heated in a heater to obtain a second heated retentate.
The second heated retentate is gasified in a gasification reactor to obtain a hot pressurized fluid mixture.
The hot pressurized fluid mixture is then transferred to the heat exchanger, where heat of the hot pressurized fluid mixture is extracted for heating the retentate to obtain a first heated retentate and to obtain a cooled pressurized fluid mixture.
The cooled pressurized fluid mixture is transferred to a pressure recovery unit and depressurized to obtain a depressurized fluid mixture.
The pressure energy of the cooled pressurized fluid mixture is recovered in the pressure recovery unit and the recovered pressure energy is partially transferred to the step of pressurizing waste water.
The depressurized fluid mixture is introduced in a separator to obtain biogas and treated water.
In accordance with one embodiment of the present disclosure, the waste water is aqueous phase obtained from hydrothermal liquefaction of biomass.
The reverse osmosis (RO) membrane has at least one configuration selected from the group consisting of hollow fiber, spiral wound and plate tube.
The first predetermined pressure is in the range of 210 bar to 280 bar, preferably 250 bar.
The gasification is optionally carried out in the presence of at least one homogeneous catalyst selected from the group consisting of sodium carbonate (Na2CO3), sodium hydroxide (NaOH), potassium hydroxide (KOH) and potassium carbonate (K2CO3).
The gasification is optionally carried out in the presence of at least one heterogeneous catalyst comprising at least one metal selected from the group consisting of Ruthenium (Ru), Rhodium (Rh) and Nickel (Ni).

BRIEF DESCRIPTION OF ACCOMPANYING DRAWING
A process and an apparatus for producing biogas from waste water organics will now be described with the help of the accompanying drawing, in which:

Figure 1 depicts an apparatus (100) for producing biogas from waste water organics in accordance with the present disclosure.

Reference number Elements
101 Pressure pump
102 Reverse osmosis unit
103 First conduit
104 Heat exchanger
105 Heater
106 Second conduit
107 Gasification reactor
108 Third conduit
109 Fourth conduit
110 Fifth conduit
111 Pressure recovery unit
112 Sixth conduit
113 Separator
114 Biogas
115 Treated water

DETAILED DESCRIPTION
Embodiments, of the present disclosure, will now be described with reference to the accompanying drawing.
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.
When an element is referred to as being "mounted on," “engaged to,” "connected to," or "coupled to" another element, it may be directly on, engaged, connected or coupled to the other element. As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed elements.
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.
Terms such as “inner,” “outer,” "beneath," "below," "lower," "above," "upper," and the like, may be used in the present disclosure to describe relationships between different elements as depicted from the figures.
The present disclosure provides a process and an apparatus for producing biogas from waste water organics. The process of the present disclosure employs hydrothermal gasification of waste water organics to obtain biogas.
In an aspect, the present disclosure provides an apparatus for producing biogas from waste water organics. Figure 1 depicts an apparatus (100) for producing biogas from waste water organics.
The apparatus (100) of the present disclosure comprises a hydrothermal liquefaction unit configured to provide aqueous phase of waste water from biomass, and a pressure pump (101) for pressurizing the waste water obtained from the hydrothermal liquefaction unit to obtain pressurized waste water. The pressure pump (101) allowing the pressurized waste water to pass through a reverse osmosis (RO) unit (102) comprising at least one reverse osmosis membrane. The RO membrane is configured for receiving pressurized waste water containing organics and allowing water to pass through it, to obtain retentate comprising organics and permeate comprising water. The retentate is transferred to a heat exchanger (104) via a first conduit (103). The retentate gets heated in the heat exchanger (104) to obtain a first heated retentate. The first heated retentate is transferred to a heater (105) via a second conduit (106). The heater (105) is configured for heating the first heated retentate to obtain a second heated retentate. The second heated retentate is transferred to a gasification reactor (107) via a third conduit (108). The gasification reactor (107) is configured for receiving the second heated retentate and gasifying the waste water organics present in the second heated retentate to obtain a hot pressurized fluid mixture. The hot pressurized fluid mixture is transmitted to the heat exchanger (104) via a fourth conduit (109) to extract heat of the hot pressurized fluid mixture for heating the retentate to obtain the first heated retentate and a cooled pressurized fluid mixture. The cooled pressurized fluid mixture is transferred to a pressure recovery unit (111) via a fifth conduit (110). The pressure recovery unit (111) is configured for receiving the cooled pressurized fluid mixture and recovering pressure of the cooled pressurized fluid mixture to obtain a depressurized fluid mixture. The depressurized fluid mixture is transferred to a separator (113) via a sixth conduit (112). The separator (113) is configured for separating biogas (114) and treated water (115) from the depressurized fluid mixture.
In another aspect, the present disclosure provides a process for producing biogas from waste water organics. The process comprises the following steps.
Waste water containing organics is pressurized at a first predetermined pressure using a pressure pump (101) to obtain pressurized waste water. The first predetermined pressure is in the range of 210 bar to 280 bar, preferably 250 bar.
The pressurized waste water is transferred through a reverse osmosis (RO) unit (102) comprising at least one reverse osmosis membrane to obtain a retentate comprising waste water organics and a permeate comprising water.
The RO membrane is designed to allow passage of water, while retaining the organics and inorganics present in the waste water. The reverse osmosis (RO) membrane has at least one configuration selected from the group consisting of hollow fiber, spiral wound, and plate tube.
The permeate can be recovered from the RO unit and the recovered permeate can be recycled and/or reused.
Due to separation of water from the pressurized waste water through RO membrane, the concentration of waste water organics in the retentate is more than that in the waste water.
In accordance with an embodiment of the present disclosure, the concentration of the waste water organics in the waste water is at least 3.3 wt% and the concentration of the waste water organics in the retentate is at least 6.5 wt%.
Thus, the recovery of the waste water organics in the retentate is in the range of 80 wt% to 98 wt% of the waste water organics present in the waste water.
The retentate containing the waste water organics is heated to obtain a heated retentate.
In accordance with one embodiment of the present disclosure, heating the retentate is carried out in two steps:
a) heating the retentate to a temperature in the range of 200 °C to 500 °C to obtain a first heated retentate;
b) heating the first heated retentate to a temperature in the range of 300 °C to 800 °C to obtain a second heated retentate.
The retentate is heated in a heat exchanger (104) to obtain a first heated retentate and the first heated retentate is heated in a heater (105) to obtain a second heated retentate.
The second heated retentate is introduced into a gasification reactor (107). The gasification reactor (107) gasifies the waste water organics in the second heated retentate to obtain a hot pressurized fluid mixture.
The process of the present disclosure can be carried out without the use of a catalyst.
Optionally, gasification is carried out in the presence of at least one homogenous catalyst selected from the group consisting of sodium carbonate (Na2CO3), sodium hydroxide (NaOH), potassium hydroxide (KOH), and potassium carbonate (K2CO3).
Optionally, gasification is carried out in the presence of at least one heterogeneous catalyst comprising at least one metal selected from the group consisting of Ruthenium (Ru), Rhodium (Rh), and Nickel (Ni).
The heat from the hot pressurized fluid mixture is extracted by passing the hot pressurized fluid mixture through the heat exchanger (104) to heat the retentate to obtain first heated retentate and a cooled pressurized fluid mixture. The cooled pressurized fluid mixture is then fed to a pressure recovery unit (111), which depressurizes the cooled pressurized fluid mixture to obtain a depressurized fluid mixture.
In accordance with the embodiments of the present disclosure, the pressure recovered from the cooled pressurized fluid mixture is partially transferred to the pressure pump (101).
The depressurized fluid mixture is then passed to a separator (113), wherein the depressurized fluid mixture is separated into the biogas and treated water.
The treated water can be recovered and can be recycled and/or reused.
In accordance with an embodiment of the present disclosure, the waste water is marine water.
In accordance with another embodiment of the present disclosure, the waste water is aqueous phase obtained from hydrothermal liquefaction of biomass.
The process of the present disclosure provides higher amount of biogas as compared to the conventional hydrothermal gasification.
The biogas obtained from the process of the present disclosure comprises higher amount of methane as compared to the conventional hydrothermal gasification.
During the process of present application, the waste water comprising waste water organics is concentrated in the RO unit before passing on to the gasification reactor. Due to higher concentration of waste water organics, the amount of energy required for the gasification of the organics is low, thereby making the process of the present disclosure more economical.
The process of the present disclosure can be carried out without the use of a catalyst. Even if, a catalyst is used, the amount thereof is less than that, the amount used in the conventional hydrothermal gasification process.
The present disclosure is further illustrated herein below with the help of the following experiments. The experiments used herein are intended merely to facilitate an understanding of the ways in which the embodiments herein may be practiced and to further enable those of skilled in the art to practice the embodiments herein. Accordingly, the experiments should not be construed as limiting the scope and scale of the embodiments herein.
Experiment 1: Treatment of marine water algal biomass for producing biogas
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.
Marine water algal biomass was first subjected to pressure pump to obtain aqueous phase marine water algal biomass, containing at least 3.3% soluble organics (waste water organics) which was used as waste water.
1885.72 Kg/hour of the waste water containing organics was pressurized using a pressure pump to obtain pressurized waste water. The pressurized waste water was fed to a reverse osmosis (RO) unit containing a RO membrane at 39 °C to obtain a retentate comprising waste water organics and a permeate comprising water. The permeate was recycled to marine water.
The retentate was heated in a heat exchanger to 442.4 °C to obtain a first heated retentate. The first heated retentate was heated in a heater to a temperature of 550 °C to obtain a second heated retentate. The second heated retentate was introduced in the gasification reactor to gasify the waste water organics present in the second heated retentate at 550 °C, at a pressure of 250 bar to obtain a hot pressurized fluid mixture.
The organics present in the retentate were converted to biogas (hydrogen, methane, CO2, CO and NH3) in the gasification reactor.
The hot pressurized fluid mixture was passed to the heat exchanger where heat of the hot pressurized fluid mixture is extracted to heat the retentate to obtain a first heated retentate and a cooled pressurized fluid mixture.
The cooled pressurized fluid mixture was transferred to a pressure recovery unit to obtain a depressurized fluid mixture. Recovered pressure energy was further used to pressurize the waste water comprising waste water organics to RO unit using the pressure pump. The depressurized fluid mixture was the fed to a gas-liquid separator, where the depressurized fluid mixture was separated into biogas and treated water. The treated water is recycled to the marine water for algal biomass growth.
The properties of the fluids at various stages within the apparatus of the present disclosure are provided in Table 1.
Table 1: Properties of the fluids at various stages within the apparatus
Temperature
(°C) Pressure
(Bar) Waste water
(Kg/h) Organics
(Kg/h) Salt
(Kg/h) Gas
(Kg/h)
Pressurized waste water organics 39 250.0 1885.725 65.355 31.682 0
Retentate (103) 39 250.0 902.980 65.34 31.682 0
Permeate 39 1.0 982.745 0.015 0.002 0
First heated retentate (106) 442.4 250.0 982.745 65.34 31.682 0
Second heated retentate (108) 550.0 250.0 982.745 65.34 31.682 0
Hot pressurized fluid mixture (109) 550.0 250.0 884.25 0 31.68 84.07
Cooled pressurized fluid mixture 60.0 250 884.25 0 31.68 84.07
Depressurized fluid mixture (112) 60.3 2.0 884.25 0 31.68 84.07
Biogas (114) 58.0 1.0 10.24 0 -- 77.33
Treated water (115) 58.0 1.0 874.0 0 31.68 6.73

It is evident from Table 1, that the waste water organics in the waste water were completely converted to biogas using the process of the present disclosure.
For comparison, gasification of the marine water was carried out using the same procedure as mentioned herein above, except that the step of passing through RO unit was not carried out. This experiment corresponds to the conventional hydrothermal gasification.
It was found that the treated water obtained from the conventional hydrothermal gasification product contains inorganic compounds and soluble oxygenated hydrocarbons such as alcohols, acids, ketones in dilute condition. Thus, during the conventional hydrothermal gasification process, the waste water organics present in the marine water provides less yield (Biogas/1000 kg waste water) of biogas. The results are summarized in Table 2.
Table 2: Comparison of conventional hydrothermal gasification with the process of the present disclosure
Product gas Unit Conventional hydrothermal gasification @1000 kg/h Process of the present disclosure @1000 kg/h
Amount of waste water organics Kg/h 33 33
65.3 (after RO)
Amount of inorganic salts Kg/h 16 16
31.7 (after RO)
Biogas obtained Kg/h 41.3 77.3
Biogas
yield /1000 kg waste water % 4.1 7.7

It is evident from Table 2 that the process of the present disclosure provides higher amount of biogas as compared to the conventional hydrothermal gasification.
The biogas obtained from the process of the present disclosure as well as that from the conventional hydrothermal gasification were analyzed. The content of biogas obtained from these two processes is summarized in Table 3.
Table 3: Content of biogas obtained using the process of the present disclosure and conventional hydrothermal gasification
Product gas Conventional hydrothermal gasification Process of the present disclosure
Mole % (Dry basis)
H2 36.4 22.9
CO 0.3 0.3
CO2 44.4 48.1
CH4 16.9 24.9
NH3 1.9 3.6
SO2 0.2 0.1

It is evident from Table 3 that the biogas obtained from the process of the present disclosure comprises 48 % more CH4 as compared to the conventional hydrothermal gasification. The amount of hydrogen in the biogas obtained by the process of the present disclosure is less as compared to that of the conventional hydrothermal gasification.
TECHNICAL ADVANCES AND ECONOMICAL SIGNIFICANCE
The present disclosure described herein above has several technical advantages including, but not limited to, the realization of a process and an apparatus:
• for conversion of waste water organics to biogas;
• for waste water treatment;
• that requires low energy for gasification of waste water organics, thereby making the entire process economical; and
• that can be carried out without use of a catalyst or using a low amount of catalyst for the hydrothermal gasification process.
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.