The present invention relates to a continuous process for producing and isolating mycoprotein from suitable culture of mycelial Fungi. In particular, the present invention relates to a more efficient and cost-effective process for producing and isolating mycoprotein.
Background
Mycoprotein is a form of single-cell protein that is typically used as a food product or ingredient. It is conventionally produced by aerobic fermentation of a carbohydrate source using filamentous fungi.
GB2137226A describes a process for producing mycoprotein by continuous aerobic fermentation using Fusarium graminearum in a culture medium containing all necessary growth promoting nutrient substances. After the mycoprotein is grown by aerobic fermentation, a heat treatment step is required to reduce the content of nucleic acid, such as RNA, present in the mycoprotein product.
GB1440642A describes a method used to reduce the content of RNA in a mycoprotein product. A heat treatment step is performed on material that has been harvested by filtration, washed and then resuspended in water. Although mycoprotein is a popular meat substitute, the production of mycoprotein is expensive. The high cost is associated with the use of refined feedstock (typically glucose syrup), high water usage, high energy costs associated with aerobic fermentation, and high plant operating costs.
US4555485 describes a method of production of an edible protein containing substance by continuous fermentation using Fusarium graminearum in a culture medium containing all necessary growth promoting nutrient substances. Oxygen constitutes the limiting nutrient and is present to support cell concentrations in the cell culture without the occurrence of anaerobic growth.
WO2016/063053 describes a process for the coproduction of mycoprotein and ethanol. In particular, mycoprotein is produced by aerobic fermentation of Fusarium species. The fermentation broth undergoes a heat treatment step to reduce RNA content and is then separated to provide mycoprotein paste and spent mycoprotein fermentation liquor. The spent mycoprotein fermentation liquor is then fed into an anaerobic fermentation process to provide ethanol. Furthermore, the heat treatment step in WO 2016/063053 can result in nutrient component interactions, such as Maillard reactions, which could negatively impact the quality and consistency of the fermentation liquor added to the anaerobic fermentation process.

US11058137 describes that the food and beverage industries produce high volumes of food grade waste streams containing starch, sugar, nitrogen and other nutrients. These are valuable food grade nutrients that we cannot afford to lose. Describing harnessing these nutrient streams and converting them into high quality food ingredients. The process also describes drying procedure at about 50°C to about 85°C using oven to obtain shelf stable food ingredient, therein the scalability of the drying process becomes an energy intensive challenge using oven. A proper drying energy efficient drying process generates stabilized product and improves the shelf life.
WO2021/123831 Al describes the use of gran feedstock and expensive enzymes to convert the cheap polymeric carbon sources to monomeric fermentable sugars and achieving specific growth rate of the mycoprotein in between 0.17 h"1 to 0.2 h"1, where the fresh media is added for 3.5 hours to provide a final biomass of concentration approximately 20 g/L.
EP3363891A1, illustrates maximal growth rates of filamentous fungi reported in submerged cultures. Industrially relevant, that means applied in thousand tons per year scale are Aspergillus niger, (citric acid), Aspergillus oryzae (food fermentations), Ashbya gossypii (riboflavin) and Fusarium venenatum, (Mycoprotein) in batch, shake flask or chemostat mode of fermentation. The temperature is 25°C with specific growth rate of the mycoprotein in between 0.17 h"1 to 0.21 h"1.
US20210137135A1, wherein fungi Aspergillus is spray dried at greater than 100°C, and wherein said dried fermented cake exhibits a moisture content of less than about 7%. The process contributes high protein content has substantially decreased antinutritional factors, reduced digestibility compared to the transferred plant - based material. Spray dryer results in a lowering of the efficiency of the Process by keeping the residence time of the droplets at a higher temperature allowing denaturation to take place thus lowering the yield of the protein component.
Additionally, the heat treatment and drying steps in typical mycoprotein production processes have high water waste.
Further, in prior art there is associated very high costs, high energy costs and high processing times.
Prior art does not specify the shelf life of the final product which is usually very less typically in hours. However in present invention the shelf life has intensively increased for storage at room temperature.
Therefore, it is an object of the present invention to provide an efficient and cost effective process for obtaining mycoprotein. The problem to be solved by the present invention is to provide a continuous

process for producing and isolating mycoprotein. In particular, the present invention relates to an efficient and cost-effective process for producing and isolating mycoprotein.
Further objects of the invention will be apparent from reading the following.
Disclosure of Invention
According to the first aspect of the invention, there is provided a continuous perfusion process for producing and isolating mycoprotein, the process comprising:
(i) Providing a fermentation substrate and fermentation media suitable for fermenting microorganism and producing mycoprotein;
(ii) Introducing the fermentation media to a fermentation vessel (flow rate); an example of introducing fermentation media to fermentation vessel by using chemostat;
(iii) Fermenting the fermentation media to obtain a mixture comprising mycoprotein and partially spent fermentation media;
(iv) Heating the mixture comprising mycoprotein and fermentation spent media; harvesting the mycoprotein as biomass;
(v) Recirculation & reintroducing the isolated partially spent fermentation media into the fermentation vessel;
(vi) Concentration of mycoprotein biomass to higher % solids through evaporation before drying; and
(vii) Using Rotary drum drying to obtain flakes (similar to spent beer yeast) as drying technology.
By the term "media" is meant a liquid designed to support the growth of microorganisms.
By the term "fermentation media" is meant media suitable for fermentation. For example, media comprising the components required to support the growth of microorganisms used for fermentation.
The fermentation substrate may comprise a carbohydrate suitable for producing mycoprotein, optionally wherein the carbohydrate is a sugar of vegetable origin, for e.g. starch, starch containing materials or products of their hydrolysis, as glucose, sucrose or a source thereof. The carbohydrate may be glucose.

Thus the substrate may comprise hydrolyzed potato, molasses, glucose, maltose, hydrolyzed bean starch or cassava.
The fermentation media may be an aqueous fermentable broth suitable for producing mycoprotein.
The fermentation media may comprise water, a carbohydrate, a source of nitrogen and nutrients. The nutrients may be suitable for producing mycoprotein. The nutrients may be selected from one or more of the group consisting of: salts, vitamins and trace metals.
The salts may be selected from one or more of the group consisting of: potassium sulphate, potassium phosphate, magnesium sulphate, manganese chloride, calcium acetate, calcium chloride, iron sulphate, iron chloride, zinc sulphate, zinc chloride, copper sulphate, copper chloride, ammonium chloride, sodium molybdate, ammonium hydroxide and ammonium phosphate.
Fermentation process - Chemostat- A perfectly mixed suspension of biomass into which a media is fed at a constant rate; and the culture is harvested at the same rate so that the culture volume remains constant. When these conditions are maintained a steady state is attained where the specific growth rate and all the parameters remain constant.
Where in, the continuous addition of fermentation medium at a flow rate (kg/h): - ((0.11-0.3) * Vf + Qevap)), where:
• Vf is the working volume in the fermenter,
• Qevap is the evaporation ratio,
A continuous harvesting at a flow rate of
= ((0.11-0.3)* Vf + Qgluc)), where
• Vf is the working volume in the fermenter,
• Qgluc is the average glucose solution flow rate

The control of an axenic, well oxygenated & aerated, nutrient rich fermentation broth (as appropriate C/N ratio, balanced nutritional conditions) is important to ensure pathways for secondary metabolite production are not activated and mycotoxins are not produced during process. Mycotoxins are secondary metabolites that may naturally be generated by Aspergillus species, Rhizopus species and Fusarium species during the fermentation process. Tight control over nutrient and oxygen levels in the fermenter ensures no mycotoxins are produced.
During its production, the fungi biomass is submitted to a heat treatment. By rapidly heating the fungal biomass (still in the broth) to temperatures above >68 °C, and keeping it for 20-45 min, the RNA content of the mycoprotein is reduced to less than 2%. The thermal treatment acts by degrading the RNA into monomers that diffuse out of the cells.
Notably, no increase in mycotoxins or microorganisms was observed in the samples.
By the term "partially spent fermentation media" is meant media that has undergone fermentation. The partially spent media may comprise at least a portion of the carbohydrate and/or nutrients from the original fermentation media. The carbohydrate may be a sugar optionally the carbohydrate may be glucose, sucrose or a source thereof.
After the portion of the isolated partially spent fermentation media is reintroduced into the fermentation vessel, the fermentation step may comprise fermenting the fermentation media and the portion of the isolated partially spent media to obtain a mixture comprising mycoprotein and partially spent fermentation media.
The fungal biomass may also be desired with increase in dry matter content and reduced moisture content. The moisture content may be less than about 20% and in some cases less than about 13% and in some case less than 6% of the biomass weight. The evaporation and concentration of biomass may be accomplished by evaporating out water from the biomass. This process may be accelerated by placing the fungal biomass in an oven, near a heat source to remove water.
Using rotary drum dryer to generate mycoprotein flakes as final product. Drying leads to the reduction of water boiling point so that the water contained in the material can evaporate below 100°C. By the decrease in the boiling point, the digestibility is maintained nutritional content such as carbohydrates, fiber, protein, and vitamins in mycoprotein are not damaged.
The continuous process may comprise:

(i) Providing a fermentation substrate and fermentation media suitable for fermenting microorganism and producing mycoprotein;
(ii) Introducing the fermentation media to a fermentation vessel; an example of introducing fermentation media to fermentation vessel is the chemostat.
(iii) Fermenting the fermentation media to obtain a mixture comprising mycoprotein and partially spent fermentation media
(iv) Heating the mixture comprising mycoprotein and fermentation spent media; harvesting the mycoprotein as biomass
(v) Recirculation & reintroducing at least a portion of the isolated partially spent fermentation media into the fermentation vessel.
(vi) Concentration of mycoprotein biomass to higher % solids through evaporation before drying
(vii) Using Rotary drum drying to obtain flakes (similar to spent beer yeast) as drying technology


Process flow diagram
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Fermentation media - A process and media composition for the growth of fusarium venenatum and production of mycoprotein is described below-
The concentration of carbohydrate in the fermentation media prior to fermentation may be from approximately 1 g/L to approximately 100 g/L, may be lOg/L to 50 g/L. The concentration of carbohydrate in the portion of the isolated partially spent fermentation media that is reintroduced into the first fermentation vessel may be less than 50 g/L.
When the nutrient is Trisodium citrate dihydrate, the concentration may be from approximately 1 g/L to approximately 10 g/L, more typically approximately 1.5 g/L to approximately 5.0 g/L.
When the nutrient is potassium, optionally potassium Nitrate, the concentration may be from approximately 1 g/L to approximately 10 g/L, typically approximately 1.5 g/L to approximately 5.0 g/L.
When the nutrient is potassium, optionally mono potassium phosphate, and the concentration may be from approximately 1 g/L to approximately 10 g/L, typically approximately 1.5 g/L to approximately 5.0
g/L.
When the nutrient is ammonia, optionally ammonium dihydrogen phosphate, the concentration may be from approximately 1.0 g/L to approximately 10 g/L, typically approximately 1.5 g/L to approximately 5.0 g/L.
When the nutrient is magnesium, optionally magnesium sulphate heptahydrate, the concentration may be from approximately 0.05 g/L to approximately 1 g/L, typically approximately 0.1 g/L to approximately 0.5

When the nutrient is calcium, optionally calcium chloride dihydrate, the concentration may be from approximately 0.01 g/L to approximately 5 g/L, typically approximately 0.05 g/L to approximately 0.25 g/L.
When the nutrient is iron, optionally iron ammonium sulphate hexahydrate, the concentration may be from approximately 0.0001 g/L to approximately 0.01 g/L, typically approximately 0.0005 g/L to approximately 0.002 g/L.
When the nutrient is citric acid, optionally citric acid mono hydrate, the concentration may be from approximately 0.001 g/L to approximately 0.01 g/L, typically approximately 0.002 g/L to approximately 0.0075 g/L.
When the nutrient is zinc, optionally zinc sulphate heptahydrate, the concentration may be from approximately 0.001 g/L to approximately O.Olg/L, typically approximately 0.002 g/L to approximately 0.075 g/L.
When the nutrient is manganese, optionally manganese sulphate monohydrate, the concentration may be from approximately 0.0001 g/L to approximately 0.001 g/L, typically approximately 0.0002 g/L to approximately 0.0005 g/L.
When the nutrient is copper, optionally copper sulphate pentahydrate, the concentration may be from approximately 0.0001 g/L to approximately 0.001 g/L, typically approximately 0.0002 g/L to approximately 0.0005 g/L.
When the nutrient is biotin, the concentration may be from approximately 0.000001 g/L to approximately 0.00001 g/L, typically approximately 0.000002 g/L to approximately 0.0000075 g/L.
When the nutrient is sodium molybdate dihydrate, the concentration may be from approximately 0.00001 g/L to approximately 0.00005 g/L, typically approximately 0.00002 g/L to approximately 0.00004 g/L.
When the nutrient is boric acid, the concentration may be from approximately 0.00001 g/L to approximately 0.00005 g/L, typically approximately 0.00002 g/L to approximately 0.00004 g/L.
In the ranges and amounts given herein it will be understood that the different values given can be combined to provide different ranges and amounts. For example, where the ranges and amounts are given as 1 g/L to 3 g/L, typically 1.5 g/L to 2.5 g/L, more typically 2 g/L, this also includes 1 g/L to 2.5 g/L, 1 g/L to 2 g/L, 1 g/L to 1.5 g/L, 1.5 g/L to 3 g/L, 1.5 g/L to 2 g/L, 2 g/L to 3 g/L, 2 g/L to 2.5 g/L, 2.5 g/L to 3 g/L and/or any other cornbrnation of values, and/or the individual values of I g/L, 1.5 g/L, 2

In the present invention, continuous fermentation is an operation which is economically competitive, where the specific growth rate is purely controlled by the feeding rate, which is very useful for growth control in industrial production. The specific growth rate achieved of the mycoprotein may be from between approximately 0.11 h"1 and approximately 03 h"1 at 30°C. Continuous fermentation has the volumetric biomass productivity in the range of 2 g/ (LH) to 6 g/ (LH). The biomass yield on glucose shows the effectiveness of each culture method on converting glucose into biomass, and such effectiveness is an important factor to consider, both technically and economically, when evaluating a fermentation process. Biomass yield on glucose consumption (g CDW/g glucose consumed) is in the range of 0.1 to 0.6. The fermentation is continued until the achieved cell biomass concentration under above defined conditions is 10 g/L to 30 g/L.
The control of an axenic, well oxygenated & aerated, nutrient rich fermentation broth (as appropriate C/N ratio, balanced nutritional conditions) is important to ensure pathways for secondary metabolite production are not activated and mycotoxins are not produced during process. Mycotoxins are secondary metabolites that may naturally be generated by Aspergillus species, Rhizopus species and Fusarium species during the fermentation process. Tight control over nutrient and oxygen levels in the fermenter ensures no mycotoxins are produced.
During its production, the fungi biomass is submitted to a heat treatment. By rapidly heating the fungal biomass (still in the broth) to temperatures above >68 °C, and keeping it for 20^5 min, the RNA content of the mycoprotein is reduced to less than 2%. The thermal treatment acts by degrading the RNA into monomers that diffuse out of the cells.
The fermentation media may be aerobically fermented with a microorganism to obtain a mixture comprising mycoprotein and partially spent fermentation media, optionally wherein the microorganism is filamentous fungi, optionally wherein the filamentous fungi is selected from one or more of the group consisting of Aspergillus species, Rhizopus species and Fusarium species. The microorganism may be Fusarium venenatum.
The process may comprise the additional step of removing the mixture comprising mycoprotein and partially spent fermentation media from the first fermentation vessel after the step of fermenting the fermentation media to obtain a mixture comprising mycoprotein and partially spent fermentation media.
The process may comprise the additional step of heating the mixture comprising mycoprotein and partially spent fermentation media.

The mycoprotein in the mixture may be a substantially solid phase and the partially spent fermentation media in the mixture may be a substantially liquid phase comprising nutrients and a carbohydrate. The step of isolating at least part of the partially spent fermentation media from the mixture comprising mycoprotein and partially spent fermentation media may comprise separating the substantially solid phase and the substantially liquid phase.
The mycoprotein can be harvested by centrifugation may be decanter centrifugation. However, any suitable centrifugation means and/or apparatus may be used. The filtration may be cross flow filtration. However, any suitable filtration means and/or apparatus may be used.
Utilization of "Pure feedstock" is undesirable cost wise. Recirculation of clarified broth to recover nutrients, the recirculation % may be from approximately 10% to approximately 95%, typically approximately 25% to approximately 90%, more typically approximately 40% to approximately 75%. In this way a significant proportion of fresh water usage is removed from the process and "waste" water and unused glucose, source of nitrogen and nutrients (that are in the at least partially spent fermentation media) can be recycled whereby reducing operation cost and waste treatment.
The step of concentration of biomass through evaporation before drying to reduce the drying capacity of the plant and therefore the investment and operation cost. There are several technologies, such as spray drying, freeze drying and solar drying have been employed to dry biomass. Rotary drum dryers are capable of drying products irrespective of moisture contents, particle sizes, and flow properties and are energy efficient that existing drying process. Drying leads to the reduction of water boiling point so that the water contained in the material can evaporate below 100°C. By the decrease in the boiling point, the nutritional content such as carbohydrates, fiber, protein, and vitamins in mycoprotein are not damaged.
The improved process as described herein provides an efficient, cost effective process for obtaining mycoprotein. The process can be incorporated into existing ethanol bio refineries, lactic acid plant, and no additional chemicals or modifications to the existing process are required. Furthermore, the waste effluent discharged from the process is significantly reduced, volume of feedstock is reduced and processing times are decreased. This results in a more efficient, cost effective and environmentally friendly process for producing mycoprotein.

What is claimed is
1. The mycoprotein comprising: mycelial fungus particles from the genus fusarium continuous perfusion media addition and continuously withdrawing a proportion of the culture at steady state from the main fermenter in the form of solids as stable powder form.
2. The fermentation process according to claim 1, wherein the mycelium fungi is Aspergillus, Fusarium or Rhizopus.
3. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Glucose lOg/L to 50 g/L.
4. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Trisodium citrate dihydrate 1 g/L to 10 g/L
5. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Potassium Nitrate 1 g/L to 10 g/L.
6. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Mono potassium phosphate 1 g/L to 10 g/L,
7. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Ammonium dihydrogen phosphate, 1.0 g/L to 10 g/L,
8. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Magnesium sulphate heptahydrate 0.05 g/L to 1 g/L,
9. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Calcium chloride dihydrate 0.01 g/L to 5 g/L,
10. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Iron ammonium sulphate hexahydrate 1 mg/L to 10.0 mg/L,
11. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Citric acid monohydrate 1 mg/L to 10 mg/L,

12. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Zinc sulphate heptahydrate 1 mg/L to 10 mg/L,
13. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Manganese sulphate monohydrate 0.1 mg/L to 1 mg/L,
14. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Copper sulphate pentahydrate 0.1 mg/L to 1 mg/L,
15. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Biotin 1 ug/L to 10 ug/L,
16. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Sodium molybdate dihydrate 10 ug/L to 50 ug/L,
17. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Boric acid 10 ug/L to 50 ug/L.
18. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Choline hydrochloride 0.01 g/L to 0.10 g/L,
19. The continuous perfusion media according to claim 1, wherein the fermentation medium has a composition comprising Phosphoric acid (85%) 0.1 g/L to 2 g/L,
20. The continuous perfusion media according to claim 1, wherein the fermentation medium has a been supplemented with Vitamins,
21. The continuous perfusion media according to claim 1, wherein in the fermentation process, the fungi solution is inoculated in an amount of 5%-10%,
22. The continuous perfusion media according to claim 1, the fermentation temperature is 25°C -32°C,
23. The continuous perfusion media according to claim 1, the pH is adjusted to 4.5 - 7.0 with aqueous ammonia,

24. The continuous perfusion media according to claim 1, the dissolved oxygen is not less than 30%-50% and the fermentation time is 86-120 hrs.
25. The continuous perfusion media according to claim 1, wherein the flow rate of sterile fresh media perfusion is in between 1.00 kg/h to about 3.00 kg/h, wherein the duration of perfusion is between 24 hour to 120 hours.
26. The continuous perfusion media according to claim 1, wherein the flow rate of perfusion of glucose is in between 0.5g/L/H to lOg/L/H, wherein the duration of perfusion is in between 24 hour to 120 hours.
27. The continuous perfusion media according to claim 1, wherein the cell growth of the fungi is at least 2-4-fold greater than the cell growth in a batch or a fed batch fermentation system,
28. The continuous perfusion media according to claim 1, where achieved cell biomass concentration is 10 g/L to 30 g/L.
29. The continuous perfusion media according to claim 1, the volumetric biomass productivity can be increased to a range of 2 g/ (LH) to 6 g/ (LH).
30. The continuous perfusion media according to claim 1, harvesting the filamentous fungal biomass and dewatering the filamentous fungal biomass to produce a harvested filamentous fungal biomass comprising about 60%-80% water and about 15%-40% filamentous fungal biomass;
31. The continuous perfusion media according to claim 1, wherein the filamentous fungal biomass slurry is grown by aerobic fermentation.
32. The continuous perfusion media according to claim 1, wherein the liquid growth medium further comprises starches, fatty acids, sugars, minerals, trace elements vitamins, extracts, or combinations thereof.
33. The continuous perfusion media according to claim 1, wherein one or more of the liquid growth medium components are derived from plant ingredients, or potato processing wastewater, or rnrn <;tillapp hvnrnrliirK

34. The continuous perfusion media according to claim 1, wherein one or more of the liquid growth medium components are derived from carbon-rich feedstock of sugar beet pulp, liquid C-starch from grain processing, vegetable waste from production of peeled, cut vegetables or rejected vegetables, lignocellulosic biomass comprises corn cobs and corn stover, Palm mill residues, including palm oil mill effluent (POME), empty fruit bunches (EFB) and palm fronds, fruit pulp, grain processing, distillation byproducts, brewing byproducts, corn stillage, potato processing waste, potato blanche water, rice processing waste, wheat straw, dairy whey, coffee processing waste, soda manufacturing waste, molasses, sugarcane bagasse, vinasse, cassava processing waste, or any combination thereof.
35. The continuous perfusion media according to claim 1, wherein the filamentous fungal particles comprise about 30%-55% protein.
36. The continuous perfusion media according to claim 1, wherein the filamentous fungal particles comprise about 30%-55% protein, with all the essential and branched chain amino acids and enhancing invitro digestibly > 90%.
37. The continuous perfusion media according to claim 1, biomass includes RNA less than lOmg- 20 mg RNA/gDCW after thermal treatment on a dry matter basis.
38. The continuous perfusion media according to claim 1, wherein the biomass is recovered from the medium by sieving, wherein the biomass was gently separated from the medium using a fine mesh sieve, whereby preferably the dry matter concentration of the sieved, biomass (cake) is at least 10%-15%(w/v).
39. The continuous perfusion media according to claim 1, wherein the biomass is recovered from the medium by filtration, wherein the biomass was gently separated from the medium using a filtration membrane, whereby preferably the dry matter concentration of the filtered, biomass (cake) is at least 10%-20% (w/v).
40. The continuous perfusion media according to claim 1, wherein the biomass is recovered from the medium by decantation's, wherein the biomass was gently separated from the medium using

decanter centrifuge, whereby preferably the dry matter concentration of the decanted, biomass (cake) is at least 15%-25% (w/v).
41. The continuous perfusion media according to claim 1, wherein the Carbon and nutrition spent media that is obtained after sieving, filtering, decanting and/or further pressing the biomass (cake) is recycled back to the fermentation and/or used for further fermentation batches.
42. The continuous perfusion media according to claim 1, wherein fungal biomass is dehydrated pellets, powder, tablets, blocks, particulates, or granules.
43. The continuous perfusion media according to claim 1, to reduce the moisture content of biomass, slurries containing not more than about 18% solids which comprises partially concentrating the slurry to a solids content in the range of 20%-40%, then further drying the hot partially concentrated still flowable slurry thereof in the range of 94%-96% and finally removing the dried solids from the drum surface.
44. The continuous perfusion media according to claim 1, where drying at temperatures e.g. >60°C is preferred.
45. The mycoprotein comprising substantially as herein described and illustrated in the drawings.