Partial-hydrothermal hydrolysis is an effective way to recover bioactives from turmeric wastes

SANTANA, Ádina Lima de; OSORIO-TOBÓN, Juan Felipe; CÁRDENAS-TORO, Fiorella Patricia; STEEL, Caroline Joy; MEIRELES, Maria Angela de Almeida

doi:10.1590/1678-457X.22016

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Research Paper • Food Sci. Technol 38 (2) • Apr-Jun 2018 • https://doi.org/10.1590/1678-457X.22016 copy

Partial-hydrothermal hydrolysis is an effective way to recover bioactives from turmeric wastes

Authorship SCIMAGO INSTITUTIONS RANKINGS

Abstract

Partial-hydrothermal hydrolysis using pressurized hot water was applied in waste turmeric, derived from extraction processes that employed supercritical and pressurized fluids, as a sustainable alternative for the recovery of bioactive constituents from this material. The reaction products consisted of a liquid extract of fermentable sugars and a solid fraction, which is a mixed biopolymer with relevant composition in terms of starch and antioxidant constituents. The effects of reaction conditions on resulting products were investigated. Economic evaluation was also performed showing that application of partial-hydrothermal hydrolysis from a residual feedstock is feasible in terms of low spend of energy and materials.

Keywords:
biowastes; carbohydrates; partial hydrolysis; phenolic compounds

Temperature (°C)		Starch (g/100 g)	AA (%)	Total phenols (g/100 g)	Total curcuminoids (g/100 g)	BDMC (%)	C (%)	DMC (%)
40	1	25 ± 2 ^a	11.72 ^a	27 ± 3^a	3.56 ± 0.009 ^a	50.10 ± 0.001	33.26 ± 0.007	16.65 ± 0.001
	2	25 ± 1 ^a	13.90 ^a	52 ± 2^a	4.94 ± 0.027^a	48.05 ± 0.011	29.30 ± 0.000	23.56 ± 0.02
	3	24 ± 2 ^a	12.72 ^a	47 ± 3^a	3.50 ± 0.002^a	50.59 ± 0.002	31.99 ± 0.001	17.49 ± 0
	4	26 ± 1 ^a	27.75 ^a	32 ± 3^a	3.34 ± 0.001^a	49.29 ± 0	33.36 ± 0	17.40 ± 0.001
	5	23 ± 0 ^a	28.25 ^a	58 ± 1^a	4.23 ± 0^a	49.64 ± 0	32.95 ± 0	17.39 ± 0
	6	25 ± 1 ^a	28.53^a	54 ± 1^a	3.72 ± 0^a	51.88 ± 0.001	31.09 ± 0.001	17.03 ± 0
	7	29 ± 1 ^a	29.37^a	39 ± 2^a	3.76 ± 0.001^a	48.84 ± 0.001	33.50 ± 0	17.63 ± 0
70	1	25 ± 2 ^a	22.59^b	25 ± 0^b	1.79 ± 0.001^a	51.32 ± 0.001	31.92 ± 0	16.84 ± 0
	2	25 ± 1 ^a	29.82^b	45 ± 0^b	2.33 ± 0.001 ^a	50.31 ± 0.001	32.67 ± 0	17.07 ± 0
	3	25 ± 2 ^a	38.40^b	59 ± 1^b	4.02 ± 0.008 ^a	50.76 ± 0.004	31.80 ± 0.003	17.67 ± 0
	4	25 ± 1 ^a	27.80^b	52 ± 0^b	3.73 ± 0.001^a	51.98 ± 0.002	30.620 ± 0.001	17.43 ± 0.001
	5	32 ± 2 ^a	30.33^b	51 ± 0^b	1.49 ± 0.002^a	48.42 ± 0.001	34.83 ± 0	16.92 ± 0.001
	6	32 ± 2 ^a	35.54^b	39 ± 5^b	3.64 ± 0.001^a	51.62 ± 0.001	31.14 ± 0	17.27 ± 0.001
	7	28 ± 0 ^a	33.74^b	46 ± 2^b	4.83 ± 0.006^a	49.89 ± 0	33.16 ± 0.005	17.11 ± 0.001
100	1	28 ± 3 ^a	33.02^b	55 ± 0^b	2.74 ± 0.010^b	55.76 ± 0.010	28.73 ± 0	15.93 ± 0
	2	30 ± 1 ^a	24.44^b	29 ± 1^b	1.29 ± 0.002^b	49.29 ± 0.001	34.39 ± 0.001	16.51 ± 0
	3	29 ± 1 ^a	16.03^b	54 ± 7^b	2.49 ± 0.001^b	51.76 ± 0.001	31.30 ± 0	16.90 ± 0
	4	29 ± 1 ^a	32.85^b	78 ± 7^b	3.17 ± 0.003^b	51.85 ± 0.001	31.37 ± 0.002	16.89 ± 0
	5	28 ± 4 ^a	30.83^b	71 ± 3^b	2.24 ± 0^b	51.48 ± 0	31.67± 0	16.85 ± 0
	6	27 ± 2 ^a	17.21^b	61 ± 1^b	2.49 ± 0^b	51.54 ± 0	31.57 ± 0.001	16.88 ± 0
	7	24 ± 0 ^a	36.49^b	64 ± 1^b	1.36 ± 0.012^b	60.32 ± 0.013	26.55 ± 0	14.02 ± 0

Temperature (°C)	Pressure (MPa)	∆H_GEL (J/g)	T_OS (°C)	T_PEAK (°C)	T_ES (°C)
Before hydrolysis		29.93	97.4	101.88	142.74
40	1	28.75	98.07	105.36	141.56
	7	27.94	97.81	105.26	147.24
70	1	29.07	97.37	104.89	140.14
	7	29.98	97.04	102.77	137.81
100	1	29.51	97.31	102.42	142.85
	7	28.97	97.53	106.94	144.53

Temperature (°C)	Pressure (MPa)	AA (%)	Total phenols (g/100g)	Total curcuminoids (g/100g)^* * Deviations lower than 0.001.	BDMC (%)	C (%)	DMC (%)
40	1	1.68^a	16±4 ^a	0.44^a	27.27	39.20	33.52
	2	0 ^a	16 ± 2 ^a	0.36 ^a	26.56	39.61	33.84
	3	12.44 ^a	7 ± 3 ^a	0.46 ^a	25.96	39.97	34.08
	4	0.50 ^a	12 ± 5 ^a	0.30 ^a	25.13	40.87	34.00
	5	7.06 ^a	11 ± 4 ^a	0.32 ^a	22.22	36.61	30.89
	6	1.18 ^a	16 ± 2 ^a	0.41 ^a	25.63	40.37	34.00
	7	0 ^a	16 ± 5 ^a	0.29 ^a	32.83	49.54	42.44
70	1	19.73^b	48 ± 1^b	0.39 ^a	28.10	41.79	35.67
	2	13.68 ^b	31 ± 3 ^b	0.35 ^a	30.05	45.90	39.23
	3	22.48 ^b	25 ± 0 ^b	0.47 ^a	32.10	51.40	43.95
	4	14.63 ^b	19 ± 1 ^b	0.41 ^a	23.68	37.65	32.80
	5	9.64 ^b	49 ± 1 ^b	0.42 ^a	24.84	39.55	34.48
	6	12.78 ^b	23 ± 2 ^b	0.44 ^a	30.15	47.06	41.37
	7	20.96 ^b	25 ± 0 ^b	0.41 ^a	35.83	53.45	46.04
100	1	13.85 ^b	27 ± 1 ^b	0.28 ^a	36.63	53.50	44.87
	2	16.03 ^b	20 ± 2 ^b	0.56 ^a	28.10	44.32	37.34
	3	7.23 ^b	25 ± 3 ^b	0.32 ^a	30.23	55.05	47.09
	4	13.12 ^b	32 ± 4 ^b	0.57 ^a	33.96	50.01	43.34
	5	13.85 ^b	34 ± 1 ^b	0.43 ^a	39.41	54.78	48.07
	6	15.92 ^b	32 ± 0 ^b	0.25 ^a	34.96	48.86	41.72
	7	12.11 ^b	38 ± 4 ^b	0.43 ^a	35.41	48.36	41.70

Equipment	$n$ ^a a n - constant depending on equipment type (Green & Perry, 2007; Silla, 2003; Smith, 1995; Turton et al., 2009);	Unit base cost (US$) ^b b Based on an operating plant with extractors of 1 L;
PLE apparatus
Storage tank	0.57	300.00
Jacketed extraction vessel ^c c Supporting pressures up to 60 MPa;	0.82	5,540.00
Electric liquid pump	0.55	3,920.00
Heater	0.59	820.00
Manometer	0	410.00
Block valve	0.60	220.00
Back-pressure valve	0.60	1,780.00
Micrometering valve	0.60	1,090.00
Flowmeter	0.60	700.00
Safety Valve	0.60	310.00
Temperature controller	0.60	310.00
Piping. connectors. crossheads. mixers and splitters ^d d Total cost.	0.60	3,660.00
Structural material for supporting the equipment ^d d Total cost.	0.60	4,060.00
Partial-hydrothermal hydrolysis	̶	23,120.00

	Industrial Units
	5 L	50 L	500 L
Fixed capital investment (FCI)
PLE apparatus ^a a Estimated cost using the Equation 5;	US$ 89,815.00	US$ 458,275.00	US$ 2,524,072.00
Depreciation rate ^b b Based on Peters et al. (2003);	10%/year	10%/year	10%/year
Annual maintenance rate ^b b Based on Peters et al. (2003);	6%/year	6%/year	6%/year
Operational labor (COL) ^c c U.S. Bureau of Labor Statistics (2015); ,^d d Turton et al. (2009);	US$ 5.95 h^-1	US$ 5.95 h^-1	US$ 5.95 h^-1
Number of workers	1	2	3
Cost of the raw material (CRM)
Water ^e e Sanasa (2015);	US$ 0.05 t^-1	US$ 0.05 t^-1	US$ 0.05 t^-1
Utilities (CUT)
Electricity ^f f U.S. Energy Information Administration (2015).	US$ 0.20 (kWh)^-1	US$ 0.20 (kWh)^-1	US$ 0.20 (kWh)^-1

Partial Hydrolysis
Size	Total Capital Investment	Operating Cost	COM TH	COM PHDDT	Cost Basis Annual Rate	Raw Material	Labor	Facility	Utilities
Size	Total Capital Investment	Operating Cost		COM PHDDT	Cost Basis Annual Rate	CMR	COL	FCI	CUT
L	US$	US$.year^-1		US$.kg^-1	kg.year^-1	%	%	%	%
5	193,000.00	108,000.00	2.56	0.90	120,010.00	0.71	63.64	35.48	0.17
50	964,000.00	361,000.00	0.96	0.31	1,166,930.00	1.97	43.6	53.96	0.47
500	5,259,000.00	1,384,000.00	0.43	0.14	10,016,624.00	4.41	17.05	77.5	1.04

T (K)	P (MPa)	T_PASTE (oC)	μ_TROUGH (cP)	μ_PEAK (cP)	μ_SETBACK (cP)	t_PEAK (min)	μ_FINAL (cP)
DDT^* * Obtained from Santana et al. (2017).
		76 ± 2	87 ± 1	87 ± 4	161 ± 3	6 ± 0	161 ± 3
313	1	76 ± 0	68 ± 0	328 ± 5	708 ± 1	6 ± 0.01	926 ± 4
	2	73 ± 2	59 ± 1	264 ± 8	547 ± 4	6.1 ± 0	607 ± 2
	3	76 ± 4	48 ± 9	209 ± 7	479 ± 9	6 ± 0	502 ± 0
	4	75 ± 2	47 ± 8	172 ± 3	375 ± 5	5.7 ± 0	420 ± 8
	5	73 ± 0	49 ± 6	153 ± 5	318 ± 1	5.3 ± 0	368 ± 0
	6	70 ± 0	54 ± 0	180 ± 7	373 ± 3	5.7 ± 0	430 ± 2
	7	73 ± 1	37 ± 2	106 ± 3	221 ± 5	5.3 ± 0	258 ± 4
343	1	71 ± 2	66 ± 0	297 ± 4	642 ± 8	6 ± 0	704 ± 8
	2	71 ± 1	76 ± 0	323 ± 6	707 ± 4	6.1 ± 0	782 ± 9
	3	74 ± 4	86 ± 7	505 ± 9	1036 ± 9	5.8 ± 0	1124 ± 7
	4	72 ± 3	64 ± 0	250 ± 8	492 ± 0	5.9 ± 0	548 ± 5
	5	78 ± 3	73 ± 0	447 ± 5	938 ± 2	5.8 ± 0	1011 ± 9
	6	71 ± 5	38 ± 4	170 ± 8	348 ± 4	5.7 ± 0	385 ± 7
	7	81 ± 3	68 ± 3	180 ± 1	294 ± 0	5.9 ± 0	382 ± 4
373	1	73 ± 0	75 ± 2	295 ± 5	604 ± 5	5.7 ± 0	683 ± 4
	2	73 ± 0	44 ± 2	147 ± 8	303 ± 1	5.8 ± 0	319 ± 2
	3	71 ± 1	75 ± 2	295 ± 5	604 ± 5	5.7 ± 0	684 ± 4
	4	69 ± 1	73 ± 0	331 ± 8	658 ± 3	5.8 ± 0	731 ± 3
	5	66 ± 1	37 ± 4	81 ± 2	123 ± 7	5.9 ± 0	160 ± 0
	6	67 ± 2	40 ± 4	102 ± 2	168 ± 1	5.7 ± 0	207 ± 4
	7	75 ± 0	51 ± 8	126 ± 2	219 ± 2	5.8 ± 0	265 ± 0

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[1] *Corresponding author: maameireles@gmail.com