Presentation Pd..Super Final Na

8/11/2019 Presentation Pd..Super Final Na

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Company Mission

Philippine Ethylene glycol Corporation (PEC)aims to be the primary ethylene glycol

manufacturer and supplier by producing high

quality products and establishing strong

connection in both local and international

markets

Company Vision

Philippine Ethylene glycol Cor(PEC) envisions itself to bec

leading ethylene glycol manu

and supplier in the Phi

providing ethylene glyc

accordance to the conforming to the demand

intermediateproduct.


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INCORPORATORS AND OFFICERS


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The plant will operate 360 days a year, 24 hours a day andays a week. Once every year during the month of Decem

allotted for the plant shutdown, which includes equipme

maintenance and repair.

The employees are required to follow the work schedule

will start from seven oclock in the morning (7:00 AM-3:0The second shift will start from 3:00 PM to 11:00 PM. Eve

will start from 11:00PM to 7:00 AM.


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ENVIRONMENTAL CONSTRAINTS Ethylene glycol is made up hydrogen, oxygen and carbon molecules. When e

oxygen with the presence of bacteria, ethylene glycol biodegrades into carbon dwater. Studies have shown that ethylene glycol is not persistent in water and bi

aerobically and anaerobically. In air, ethylene glycol is not readily volatile and photochemical oxidation; ethylene glycol atmospheric half-life as approximately

Ethylene glycol can be disposed off and treated in conventional waste water plants.


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ECONOMIC CONSTRAINTSIn the production of ethylene glycol, it requires large amount of water and

to meet the needed performance of each equipment. With this, the supplies a

sure to be in allowable quantities with standby support like generators in casfailure and storage tanks to store more water. The plant site was also located

special economic zone area in Mabalacat Pampanga where enough water sup

provided.


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HEALTH AND SAFETY CONSTRAINTS While ethylene oxide as the raw material is very toxic, fatal if inhaled, may cause

respiratory irritation, drowsiness and dizziness, corrosive, causes severe skin burnsdamage,cancer and may damage fertility and cause genetic defects.

The risk of accidental exposure to these chemicalsshould be controlled by selectinapplying the appropriate Risk Management Measures.Safety measures are also

implemented to the work place. Posters and instructions are posted to the workingMSDS and first aid measures for these are provided.The companyalso trains every

personnel as part of the companys effective risk management program to avoid anincidents that may occur in the production site.


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MANUFACTURABILITY AND SUSTAINABILITY CONSTRAINTSAccess to an adequate supply of parts and raw materials has to be consideralso. A business that is able to supply appropriate quantities of goods and se

to customers 'just in time' also needs to have access to supplies and materia

in time'. To make this possible the company maintains its good relationship

suppliers of raw materials and its target clients. And in order to access supp

in time, plant cite was located to a special economic zone area inMabalacat

Pampanga which are near to coastal port areas since the raw materials are timported in nearest possible suppliers from nearby countries like China and

Singapore, this is to lower the cost of transportation and delivery charge of t

raw materials.


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ETHICAL AND PROFESSIONAL CONSTRAINTS

The company follows the standards and rules set by the Department of Labo

Employment in the protection of labor in the promotion of full employment and assurance of equal opportunities regardless of race, gender and beliefs. The emp

and laborers will be treated fairly and equally and their voice will be heardcompany will have an Employee of the Month, to recognize their valuable contri

to the company and to motivate every employee to contribute to the achievemcompany visions.

The company will apply for ISO 9001:2008 certifications to assure the clienbusiness partners that the company increases its effectiveness and efficiency tcontinual improvement in systems and products/ service quality. Throug

certification also, the company will able to prove that it is a customer-foorganization.


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Four Mathematical Methods Description

Arithmetic Straight Line Method(ASLM) Arithmetic Straight Line Method (ASLM) assumes t

annual increase in the future will be the same alt

the rate or increase in percent will keep on going

Arithmetic Geometric Curve

Method(AGCM)In this method, the rate of increase in the projec

values is constant; however, the amount of chang

on increasing.

Statistical Straight Line Method (SSLM) For this method, the change in the figure is unifo

while the change as a % of the data for the year idecreasing.

Statistical Parabolic Curve Method

(SPPM)In SPPM, the change in the predicted values may increasing or decreasing while the percentage ch

the values for the prior year may also be increasidecreasing.


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Historical Demand for Ethylene Glycol

Year Net Weight (kg)

2004 9989351

2005 15207516

2006 14461181

2007 17580530

2008 18073862

2009 20305136

2010 23812732

2011 25812732

2012 30557942

2013 34461181


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Historical supply for Ethylene GlycolYear Net Weight (kg)

2004 3884723

2005 3945672

2006 4831932

2007 7580530

2008 9073863

2009 11305136

2010 14897363

2011 15449435

2012 19586636

2013 22869352


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Graphical representation of the historical

demand of Ethylene Glycol [national statisticsoffice (NSO) public reference unit, 2014]

0

5000000

10000000

15000000

20000000

25000000

30000000

35000000

2004 2005 2006 2007 2008 2009 2010 2011 2012 2013

NetWeightin(kg)

Year


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Graphical Representation of the HistoricalSupply of Ethylene Glycol [Securities andExchange Commission, Public Reference

Unit, 2014]

0

5000000

10000000

15000000

20000000

25000000

2004 2005 2006 2007 2008 2009 2010 2011 2012 2013

NetWeight

(kg)

Year


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Graphical Representation of the Behavior of the Historical Demand and Supply of Eth

Glycol

0

5000000

10000000

15000000

20000000

25000000

30000000

35000000

40000000

2004 2005 2006 2007 2008 2009 2010 2011 2012 2013

N

etWeight(kg)

Year

Supply Demand


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Historical Demand for Ethylene Oxide

Year Weight (kg)

2004 70,335,973

2005 71,771,401

2006 73,236,123

2007 74,730,738

2008 76,255,855

2009 77,812,097

2010 79,400,099

2011 81,020,510

2012 85,567,875

2013 87,693,596


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HISTORICAL SUPPLY FOR Ethylene Glycol

Year Weight (kg)

2004 80,445,597

2005 79,558,459

2006 78,258,386

2007 79,739,329

2008 85,255,855

2009 79,812,097

2010 85,438,732

2011 88,020,510

2012 93,495,938

2013 90,748,864


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Historical Demand for Ammonia

Year Weight (kg)

2004 93337297

2005 98249787

2006 103420828

2007 108864030

2008 1145937152009 120624964

2010 126973646

2011 133656470

2012 137667870

2013 141983340


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HISTORICAL SUPPLY FOR AMMONIA

Year Weight (kg)

2004 86674594

2005 96499574

2006 106841656

2007 117728060

2008

119187430

2009 121249928

2010 133947292

2011 137312940

2012 145335740

2013 153966680


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Graphical Representation of the Demand of Ethylene

Oxide [National Statistics Office (NSO) PublicReference Unit, 2014]

0

10,000,000

20,000,000

30,000,000

40,000,000

50,000,000

60,000,000

70,000,000

80,000,000

90,000,000

2004 2005 2006 2007 2008 2009 2010 2011 2012 2013

N

etWeight(kg)

Year


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Projected Demand and Supply of Ethylene Glycol for the Next Ten Years Us

Statistical Parabolic Projection Method and Statistical Straight Line Method

Year Demand (kg) Supply(kg) Difference(kg)

2014 37,894,420.62 26,459,556.07 11,434,864.55

2015 42,181,500.70 30,370,482.59 11,811,018.11

2016 46,773,614.25 34,572,000.20 12,201,614.05

2017 51,670,761.27 39,064,108.90 12,606,652.37

2018 56,872,941.74 43,846,808.70 13,026,133.04

2019 62,380,155.68 48,920,099.58 13,460,056.10

2020 68,192,403.08 54,283,981.56 13,908,421.52

2021 74,309,683.94 59,938,454.62 14,371,229.32

2022 80,731,998.26 65,883,518.78 14,848,479.48

2023 87,459,346.04 72,119,174.03 15,340,172.01


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Graphical Representation of the Projected Demand and Sup

Ethylene Glycol

0.00

10,000,000.00

20,000,000.00

30,000,000.00

40,000,000.00

50,000,000.00

60,000,000.00

70,000,000.00

80,000,000.00

90,000,000.00

100,000,000.00

2014 2015 2016 2017 2018 2019 2020 2021 2022 2023

NetWeight(kg)

Year

Demand

Supply


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Projected Demand and Supply of Ethylene Oxide for

the Next Ten Years Using Statistical ParabolicProjection Method

Year Demand (kg) Supply(kg)

2014 110795095 121360878

2015 119243683 130177791

2016 127879141 139150392

2017 136701467 148278680

2018 145710662 1575626562019 154906727 167002320

2020 164289660 176597671

2021 173859462 186348711

2022 183616134 196255438

2023 193559674 206317853


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Graphical Representation of the ProjectedDemand and Supply of Ethylene Glycol

0

50000000

100000000

150000000

200000000

250000000

2014 2015 2016 2017 2018 2019 2020 2021 2022 2023

Net

Weight(kg)

Year

Demand

Supply


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13-Nov-13 17-Feb-14 24-May-14 28-Aug-14 2-Dec-14 8-Mar-15 12-Jun-15 16-Sep-15 21-Dec-15 26-Mar-16 30-J

Feasibility Study and Project Planning

Incorporation

Financial Acquisition

Plant Site Negotiation

Plant Size Acquisition

Preparation of Engineering Design and Specification

Plant Construction Bidding

Plant Construction

Order and Fabrication of Equipment

Equipment Arrival

Hiring of Personnel

Installation of Equipment

Order and Delivery of Raw Materials

Training of Personnel

Trial Run

Advertising and Promotion

Start of Normal Operation

Plant SiteNegotiation

Plant SizeAcquisition

Preparation ofEngineeringDesign and

Specification

PlantConstruction

Bidding

PlantConstruction

Order andFabrication of

Equipment

EquipmentArrival

Hiring ofPersonnel

Installation ofEquipment

Order andDelivery of Raw

Materials

Training ofPersonnel

Trial RunAdvertising and

PromotionStart of Normal

Operation

Start Date 7-Apr-149-Jun-145-May-145-May-1415-Aug-145-May-145-Jan-155-Oct-145-Jan-154-Jun-158-Jun-157-Sep-157-Sep-156-Mar-16

Duration 635691311153081202431509591181181365


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Process 1Manufacturing acrylonitrile by combining propylene, am

and air in a process called ammoxidation. During

ammoxidation, propylene, ammonia and air are fed thr

catalyst at a high temperature. The vessel containing t

chemical reaction is called a fluid bed reactor, where tpowdered catalyst moves fluid-like throughout the reac


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Process 2Manufacture of Acrylonitrile from Ethylene Cyanohydrin

Germany and the United States first produced acrylonitrile on

industrial scale in the early 1940s. These processes were base

catalytic dehydration of ethylene cyanohydrin. Ethylene cyan

was produced from ethylene oxide and aqueous hydrocyanic aC in the presence of a basic catalyst. The intermediate was t

dehydrated in the liquid phase at 200 C in the presence of m

carbonate and alkaline or alkaline earth salts of formic acid.


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Process 2

Manufacture of Acrylonitrile from Ethylene Cyanohydrin


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Process 3Manufacturing of Acrylonitrile from Acetylene and HydroAcid

Catalyst consisting of cuprous chloride and ammonium chlorid

solution in hydrochloric acid. A large excess of acetylene is us

15 mol/mol HCN) at a pressure slightly above 0.1106 pa absotemperature of 80 to 90C.

The molar yield is up to 90 per cent in relation to hydrogen c

and 75 to 80 per cent in relation to acetylene. The main by-p

are acetaldehyde, vinyl acetylene, divinyl acetylene, vinyl ch

cyano butene, lacto-nitrile, methyl vinyl ketone, etc.


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Areas of

Concern

Process 1: SOHIO Process (Manufacture of Acrylonitrile by

Ammoxidation of Propylene) Process 2: Manufacture of Acrylonitrile from Ethylene

Cyanohydrin

Process 3

RAW

MATERI

ALS

Propylene, Ammonia, Air Catalyst: Bismuth MolybdateEthylene Cyanohydrin Catalyst: Sodium Formate Acety

NO .

OF

EQU

IPMEN

T

10 9

ADVANTAGES Single step

Process

Maximum Yield

Less Expensive

Useful by- products

Assures high yields of acrylonitrile

Few Impurities Good re

DISADV

ANTAG

E

It hasnt been used in the manufacturing industry sinceSOHIO Process

Materia

Large n

More ca HCN is

Build u

chlorid

-

Hydrogen Cyanide, Acetonitrile, Carbon OxidesAcetald

AVA

ILABILITYOFRAW

MATERIALS

The supply of propylene from different companies for the last tenyears to the different countries in the world indicates that there

is a sufficient supply of propylene and ammonia which can be used in the

manufacturing process.

(United Nations Commodity Trade Statistics Database (UNCOMTRADE),

2014)

Imports: of ethylene oxide are relatively small, with amounts

increasing from 1982 to

1984 from 4,300 kkg to

5,600 kkg. Exports: of ethylene

oxide increased substantially over the same period, from 1,500

kkg in 1982 to 11,200 kkg in 1984 (SRI 1984).

2002: 1,

1,870 milli

trade in HC

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Transportation facilities available- Transportation access to wider marke

economic scale in production, distribution, and consumption, thereforetransportation increasing economic growth.

Accessibility to the target market- Accessibility to the target markets af

cost of the product and it requires a lot of time for distribution.

Water source quality and quantity- Numerous plant uses large amount ofoperating plant and some operations that needed the supply of water.

Special business incentives-Incentives create a good relation to the man

and the consumers

Climatic conditions-Climate affects the operation of the plant, the prod

transportation of the raw material and the products.


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Utilities costs and availability-Plant operations are dependent to the fue

electricity; therefore utilities should take into consideration Treatment facility- The location of the plant should have a correct wast

and treatment facility because it is one of the requirements by the law.

Construction cost- Cost of the construction includes the equipment, the

construction of the plant, and the land.

Operating labour- It will determine the number of manpower that is beithe operation of the plant.

Taxes- Taxes will affect the business in one way or other

Living conditions and expansion possibilities- The chosen location must b

zone and have large area for future expansion and development consideprojected business growth


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TIPCO Estates corporation (TECO) Special Economic Zone, Mabal

Pampanga, Philippines


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The First Cavite Industrial Estate (FCIE) situated in Lankaan, Dasmarin

In Cavite.


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Criteria % (TECO)Pampanga

(LISP)Batangas

(FCCav

Transportation Facilities 10 8 7Accessibility to Target Markets

10 8 7

Water source quality and quantity

10 8 8Special Business Incentives

10 9 9Climatic Conditions

10 8 6Utilities Costs And Availability

10 7 7Treatment Facility

10 7 7Construction Cost

5 5 5Operating Labour

10 8 8Taxes

5 4 4Living conditions/expansion

possibilities10 9 8

Total 100 81 76


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Formula C2H6O2

IUPAC ID Ethane-1,2-dio

Molecular Weight g/mol 62.07

Boiling point at 101.3 kPa 197.60 C

Freezing point -13.00 C

Density at 20C 1.1135 g/cm3

Heat of vaporization at 101.3 kPa 52.24 kJ/mol

Heat of combustion 19.07 MJ/kg

Critical temperature 372 C

Critical pressure 6515.73 kPa

Critical volume 0.186 L/mol

Flash point 111 C

Ignition temperature 410 C

Lower explosive limit 3.20 vol%

Upper explosive limit 53 vol%

Viscosity at 20 C 19.83 mPa.s

Cubic expansion coefficient at 20 C 0.6210-3 K-1


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Ethylene Glycol= 5

Water= 15675.2 kg

Higher Glycol= 10

Ethylene Oxide= 8

Ethylene Oxide = 4252.844 kg

Water = 17397.56 kg

Components Mass In Mass out

Ethylene Oxide 4339.6367 86.7927

Water 17397.56 15675.2

EG 5872.748

Higher Glycol 102.4544

Total 21650.41 21650.41

Assumptions:1. No accumulation

2. Selectivity is 98%3. Percent excess water is 20%

4. Ratio of water to Ethylene Oxide 9.8:15. 98%

C2H4O + H2O

C2H4O + C2H6O2

ReactionsInvolved:


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1. Accumulation equals 0.01%

2. Consider the water content of glycol is

reduced from 72.4 % to 65.56%.

Feed Mass(kg)

EO 86.7927

Water 15675.2

MEG 5872.748

DEG 102.4544

Total 21737.1951

Components Mass(k

Water 11210.

MEG 5787.0

DEG 102.44

Total 17100.

Components Mass(kg)

EO 86.784

Water 4462.895

EG 85.07

Total 4634.729

Calculation:

F = V + L+ Accumulation

F = V + L +0.0001(F)

21737.1951= 4634.729+ 17100.27241+

0.0001(21737.1951)

2 2 EQUIPMENT: TRIPLE EFFECT EVAPORATOR


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2.2 EQUIPMENT: TRIPLE EFFECT EVAPORATOR

SECOND EFFECTComponents Mass(kg)

Water 4462.895

MEG 85.07

total 4547.945

Feed

Components Mass(kg)

Water 11210.73748

MEG 5787.090725

HG 102.444203

Total 17100.27241

Components

Water 67

MEG 57

HG 10

total 125


2. Consider the water content of glycol isreduced from 65.56% to 53.756%.

Calculation:


F = V + L +0.0001(F)

17100.27241= 4547.945+ 12550.59736+

0.0001(17100.27241)

17100.27241= 17100.27241

2. 3 EQUIPMENT: TRIPLE EFFECT EVAPORATOR


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THIRD EFFECT

Components Mass(kg)

Water 6746.7214

MEG 5701.4420

HG 102.43396

total 12550.597Components mas

Water

MEG

HG

total

Components mass(kg)

Water 4462.895

MEG 85.07

Total 4547.945


2. Consider the water content of glycol is

reduced fr om 53. 75 6% to 28.5%.

Calculation:


F = V + L +0.0001(F)

12550.597= 4547.945+ 8001.856 + 0.0001(12550.597)

12550.597= 12550.597


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Suppose MEG is concentrated from 27.125 % to70.18 % in this triple effect long tube verticalfalling film evaporator.

Components Mass %Mass

Water 15675.2 72.401

Ethylene Glycol 5872.748 27.125

Di-ethylene Glycol 102.4544 0.4732

Total 21650.41 100

Components Mass %Mas

Water 2283.626 28.53

Ethylene Glycol5615.807

70.18

Di-ethyleneGlycol 102.4237

1.279

Total 8001.856 100

Material Entering the Evaporator

Material Leaving the Evaporator (Bottom Product Concentrate)


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Bottom Mass(kg)

MEG 5568.64523

DEG 102.4134733

total 5671.058712

Feed Mass(kg)

Water 2283.626

MEG 5615.807

HG 102.4237

Total 8001.856

Components M

Water 2283

MEG 46

Total 232

Data and Assumptions:1. Accumulation equals 0.01%Components Mass(kg)

Calculation:

F = D + B+ Accumulation

F = D + B +0.0001(F)

8001.856= 2329.99755+5671.0587+ 0.0001(8001.856)


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Data and Assumptions:


2. 99.8% purity of ethylene glycol is drawn out in the distillate.

feed mass(kg)

MEG 5568.645239

HG 102.4134733

total 5671.058712

Distillate Mas

MEG 5506HG 11.0

total 551

Bottom

Components Mas

MEG 61.1

HG 91.3

Total 152

Calculation:


F = D + B +0.0001(F)

5671.0587= 5517.94+152.5515+ 0.0001(5671.0587)

5671.0587= 5671.0587


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1. Accumulation equals 0.01%2. 99.9% purity of water is drawn out in

the distillate.

Feed mass

EO 86.784

MEG 301.81

water 15671.77

total 16060.364

Distillate mass(kg)

EO 86.7753

water 15174.57MEG 9.58415

total 15270.91

Bottom

masMEG 292

water 4

total 787

Calculation:


F = D + B +0.0001(F)

16060.364= 15270.915+787.8357 + 0.0001(16060.364)

16060.364= 16060.364

TABLE OF STANDARDS

C d D i ti


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Code Description

Batas Pambansa Bilang 68 Corporation Code of the Philippines Articles o

Republic Act No. 8749 Philippine Clean Air Act of 1999 Wast

Republic Act No. 9275 Philippine Clean Water Act of 2004 Wast

Presidential Decree No. 984 Pollution Control Law of 1976 Wast

DENR Administrative Order No. 90-35 Revised Effluent Regulations of 1990 Wast

Presidential Decree No. 856 Sanitation Code of the Philippines Wast

Presidential Decree No. 442 The Labor Code of the Philippines Manag

OSHA Occupational Safety and Health Administration Health

NIOSH National Institute of Occupational Safety and

Health

Health

Presidential No. 442 Labor Code of the Philippines Management Stu


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Presentation Pd..Super Final Na

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