This document provides information about a company called Joint Stock Company "GTL" including its legal details, capital structure, brief reference, and a project to build an industrial plant in Bratsk Gas Condensate Field. The key details are:
- JSC "GTL" was founded in 2000 to develop a technology for direct synthesis of alcohols from natural gas and processing them into engine fuels.
- The project aims to build a plant with capacity of 100,000 tons per year to process natural gas from Bratsk Gas Condensate Field into gasoline.
- The technology is unique as it allows refining of gas into liquid fuels at any pressure, without needing compression equipment. This
Sweetening and sulfur recovery of sour associated gas and lean acid gas in th...Frames
Effective and efficient removal of hydrogen sulfide (H2S) is an essential step when sweetening gas for downstream processes. By simultaneously turning the captured hydrogen sulfide into elemental sulfur, a Frames THIOPAQ O&G system improves gas value, while creating a saleable chemical widely sought after in the agricultural and bulk chemical industry.
This is a presentation on the design of plant for producing 20 million standard cubic feet per day (0.555 × 106 standard m3/day) of hydrogen (H2) of at least 95% purity from heavy fuel oil (HFO) with an upstream time of 7680 hours/year applying the process of partial oxidation of the heavy oil feedstock.
all process involve in petroleum to get final products from crude oil like LPG, petrol, diesel, jet fuel, kerosene,neptha, heavy neptha, coke and petroleum products
The impact of engine operating variables on emitted PM and Pb for an SIE fuel...iosrjce
The replacement of gasoline with ethanol is increased worldwide indicating the need to understand
the air quality impacts of this exchanging. In the recent study, variable experimental tests conducted to evaluate
the impacts of several ethanol-gasoline blends (E20, E50, and E80) on particulate matter (PM) and lead (Pb)
concentrations emitted from a four-stroke, single cylinder, water-cooled spark-ignition (SI) engine. PM and Pb
exhaust emissions measured and analyzed at variable engine operation parameters.
The emitted PM emissions reduced with increase concentration of ethanol in the blend. Compared to the
baseline gasoline (E0), E20 gave relatively lower reductions in PM emissions, while E50 and E80 both reduced
PM emissions under the conditions studied. Ethanol was observed to impact Pb emissions depending on the
ethanol share in the blend
Introduction and Theoretical Aspects
Catalyst Reduction and Start-up
Normal Operation and Troubleshooting
Shutdown and Catalyst Discharge
Nickel Carbonyl Hazard
Modern Methanation Catalyst Requirements
Sweetening and sulfur recovery of sour associated gas and lean acid gas in th...Frames
Effective and efficient removal of hydrogen sulfide (H2S) is an essential step when sweetening gas for downstream processes. By simultaneously turning the captured hydrogen sulfide into elemental sulfur, a Frames THIOPAQ O&G system improves gas value, while creating a saleable chemical widely sought after in the agricultural and bulk chemical industry.
This is a presentation on the design of plant for producing 20 million standard cubic feet per day (0.555 × 106 standard m3/day) of hydrogen (H2) of at least 95% purity from heavy fuel oil (HFO) with an upstream time of 7680 hours/year applying the process of partial oxidation of the heavy oil feedstock.
all process involve in petroleum to get final products from crude oil like LPG, petrol, diesel, jet fuel, kerosene,neptha, heavy neptha, coke and petroleum products
The impact of engine operating variables on emitted PM and Pb for an SIE fuel...iosrjce
The replacement of gasoline with ethanol is increased worldwide indicating the need to understand
the air quality impacts of this exchanging. In the recent study, variable experimental tests conducted to evaluate
the impacts of several ethanol-gasoline blends (E20, E50, and E80) on particulate matter (PM) and lead (Pb)
concentrations emitted from a four-stroke, single cylinder, water-cooled spark-ignition (SI) engine. PM and Pb
exhaust emissions measured and analyzed at variable engine operation parameters.
The emitted PM emissions reduced with increase concentration of ethanol in the blend. Compared to the
baseline gasoline (E0), E20 gave relatively lower reductions in PM emissions, while E50 and E80 both reduced
PM emissions under the conditions studied. Ethanol was observed to impact Pb emissions depending on the
ethanol share in the blend
Introduction and Theoretical Aspects
Catalyst Reduction and Start-up
Normal Operation and Troubleshooting
Shutdown and Catalyst Discharge
Nickel Carbonyl Hazard
Modern Methanation Catalyst Requirements
A minor presentation report based on the development of electrolyzer for hydrogen production.
And burning the produced hydrogen along with petrol air mixture or charge in SI Engine.
Explaining the major changes obtained in the fuel emission as well the performance of vehicle
GE / Texaco Gasifier Feed to a Lurgi Methanol Plant and its Effect on Methano...Gerard B. Hawkins
GE / Texaco Gasifier Feed to a Lurgi Methanol Plant and its Effect on Methanol Production
CONTENTS
0 Methanol Synthesis Introduction
1 Executive Summary
2 Design Basis
2.1.1 Train I Design Basis
2.1.2 Train II Design Basis
2.1.3 Train III Design Basis
2.2 Design Philosophy
2.2.1 Operability Review
2.3 Assumptions
2.4 Train IV Flowsheet
2.4.1 CO2 Removal
3 Discussion
3.1 Natural Gas Consumption Figures
3.1.1 Base Case
3.1.2 Case 1 – Coal Gasification in Service
3.1.3 Case 2 – Coal Gasification in Service – No CO2 Export
3.2 Methanol Production Figures
3.2.1 Base Case
3.2.2 Case 1 – Coal Gasification in Service
3.2.3 Case 2 – Coal Gasification in Service – No CO2 Export
3.3 85% Natural Gas Availability
3.4 100% Natural Gas Availability
3.5 CO2 Emissions
3.5.1 Base Case
3.5.2 Case 1 – Coal Gasification in Service
3.5.3 Case 2 – Coal Gasification in Service – No CO2 Export
3.6 Specific Consumption Figures
3.6.1 Base Case
3.6.2 Case 1 – Coal Gasification and CO2 Import
3.6.3 Case 2 – Coal Gasification and No CO2 Import
3.7 Train IV Synthesis Gas Composition
4 Further Work
5 Conclusion
APPENDIX
Important Stream Data – Material Balance Stream Data
Texaco Gasifier with HP Steam Raising Boiler
CHARACTERISTICS OF COAL
Material Balance Considerations
SYNGAS CONDITIONING UNIT FEASIBILITY CASE STUDY: COAL-TO-LIQUIDSGerard B. Hawkins
SYNGAS CONDITIONING UNIT FEASIBILITY CASE STUDY: COAL-TO-LIQUIDS
Case Study: #0953616GB/H
HT SHIFT REACTOR CATALYST SPECIFICATION
Process Specification
This process duty specification refers to a Syngas Conditioning Unit which utilizes HT Shift reaction technology on a slip stream of raw gas to produce a recombined gas stream with a H2:CO ratio of 1.57:1. This is an important consideration as the Shift reactor is not required to minimize CO at outlet, and this specification refers to the expected performance that can be achieved in a single stage reactor scheme.
The Syngas Conditioning Unit is part of a proposed coal-to-liquids complex in which synthesis gas is produced by gasification of coal for downstream processing in a Fischer Tropsch reactor and Hydrocracker unit.
Due to its impact on human health and the nature surrounding us, diesel engine emissions have been significantly reduced over the last two decades. This reduction has been enforced by the legislating organs around the world that gradually have made the manufacturers transform their engines to today’s complex high‐tech products. One of the most challenging area to meet the legislations is the emissions of the diesel engine which are the products of the combustion of diesel fuel. More restrictions have been imposed by the some governments to reduce these emissions to a level such that will not cause any harmful impacts for the environment after releasing them to the atmosphere. This paper examines the effects of combusting a mixture of diesel fuel, water, and surfactant which forms emulsion on the nitrogen oxides, or NOx, carbon monoxide CO, carbon dioxide CO2, sulfur oxides SOx emissions and particulate matter (PM) from a compression ignition diesel engine. Previous research has attributed the observed reduction of these emissions to a suppression of flame temperature due to quenching effects from the water, thereby reducing thermal NOx formation and other pollutants. The focus of this review paper will be on experiments were conducted a using diesel engine with pure diesel fuel and emulsion of water-diesel. Furthermore, results from the testing diesel fuel that mixed with varied ratios of water balanced with a surfactant to stabilize the emulsion will be presented and discussed. Three different samples of water- diesel emulsion were used with 10 % water and 90 % diesel, 20 % water and 80% diesel, and 30 % water and 70 % diesel (by volume) respectively to conduct the experiments in the lab . The purpose was to see the impact of adding the water from 10 % up to 30 % (by volume) to the diesel fuel making the emulsion fuel to explain what will occur to the emissions and the performance of the engine. The data shows significant NOx emission reduction when using the emulsion water diesel fuel of 30 % water (by volume) in diesel. These results are correlated with a thermodynamic first law analysis to estimate the adiabatic flame temperature of the standard fuel and fuel-water emulsion cases. Results indicate that thermal NOx is indeed reduced by quenching and flame temperature suppression confirming reports in the literature. Recommendations are given for further studies, including improving the fuel—water emulsion and considerations for long-term testing.
Similar to TECHNOLOGY FOR ALCOHOLS DIRECT SYNTHESIS FROM GAS PROCESSING ALCOHOLS INTO MOTOR FUEL (20)
TECHNOLOGY FOR ALCOHOLS DIRECT SYNTHESIS FROM GAS PROCESSING ALCOHOLS INTO MOTOR FUEL
1.
2. COMPANY INITIATING PROJECT REFERENCE
Full name of the company:
Legal address:
Location address:
Main state registration number:
Main activity:
Taxpayer identification number:
Management:
Shareholder's capital:
IPO:
Joint Stock Company “GTL”
125047, Gasheka Street 8-10, build. 8, Moscow
117246, Nauchniy driveway 8, build. 1, Moscow
1027700525181
engineering and technical activity
7706211944
Kadyrov Rafis Faizovich, President of the Company
519 200 000 rubles
February 2013, Moscow Central Stock Exchange
JSC “GTL” CURRENT CAPITAL STRUCTURE
Registered capital
Fixed assets:
— intangible assets
— research and developments results
Current assets:
— recurring operations
519 200 000 rubles
27.04 billion rubles, including:
24.9 billion rubles
2.14 billion rubles
1.64 billion rubles, including
1.54 billion rubles
3. JSC “GTL” BRIEF REFERENCE
JSC “GTL” was founded in 2000 in order to realize a project of extinguishing flares
and refining natural gas into high-octane engine fuels (petrol and diesel fuel)
avoiding the stage of synthesis gas in the technological process. To fulfill this task
the company has worked out the technology for direct synthesis of alcohols with
their further processing into motor fuel.
The technology is unique due to its high profitability, possibility of refining gas
containing any components with isolating end-product (high-octane petrol, diesel
fuel, methanol, ethanol, helium).
JSC ''GTL'' has invested in R&D aimed at creating this technology 2.139 billion
rubles by 2013, the project is at the stage of building industrial plant.
At the present moment JSC “GTL” in the frames of agreement with JSC “Rosneft” and “ITERA Oil-and-gas company” Ltd. has
started building the plant with capacity 100 thousand tons per annum in the territory of Bratsk Gas Condensate Field
(Krasnoyarsk Territory). The first stage of the project is planned to be launched in May 2014.
4. PROJECT BRIEF DESCRIPTION
AIM OF THE PROJECT
PRODUCTS
TARGETS OF
THE PROJECT
Creating business structure which will provide processing natural and associated gas on the
base of low-tonnage automated unitized GTL plants
Low-tonnage automated unitized GTL plants. The distribution area for the products of the
project is represented by oil companies
Cost efficient development of small and middle gas fields and gas-condensate fields
Processing associated gas in oil fields
Creating and developing market for low-tonnage automated unitized plants of synthetic
liquid fuels
Recycling associated gas for oil production
Monetisation of gas in remote and low-pressure fields
Monetisation of remote shale gas fields
Processing gas into liquid on sea-based platforms
PROJECT STATUS
Current stage of the project (August 2013)
Planned stage of the project (February 2014)
THE STAGE OF DESIGNING
THE STAGE OF THE FIRST INDUSTRIAL LAUNCH
The technical documentation of the petrol synthesis block
of the plant with capacity 100 thousand tons per annum
(for the gas of Bratsk Gas Condensate Field) is prepared.
The preparation for testing pilot plant of direct alcohols
synthesis (1000 tons of methanol) is being terminated.
The launch of pilot plant of direct alcohols synthesis with
capacity 1000 tons of methanol per year to receive
350-420 tons/year of certified gasoline 95 octane per annum.
5. PLANT BUILDING IN BRATSK GAS CONDENSATE FIELD
The aim of this project is building the industrial complex for processing 146 million m3 of natural gas into 100 000 tons of
certified gasoline 95 octane of standard RON 5 and Euro 5 standard.
The cost of the project is 2 300 000 million rubles. The project is fulfilled at the expenses of the company and with the use of
credit financial resources.
The terms for realization of the project: 12 months.
The fixed terms include design, production of the equipment, installation, putting the plant into operation.
PROJECT EFFICIENCY INDICES
Efficiency Final Indices
28 quarters
Discount rate
15%
IRR (Internal rate of return)
79%
NPV, rubles.
Simple payback period of the project, years
Investments in capital assets, rubles
3 686 979 127
2.25
2 300 000 000
6. PRODUCTS COST
Service Name
Price
Automobile certified gasoline 95 octane of Еuro 5 standard
30 000 RUB/ton
PRODUCTS PRIME COST
Service Name
Price
Automobile certified gasoline 95 octane of Еuro 5 standard
5 000 RUB/ton
PRODUCED PETROL VOLUMES
Service Name
Automobile gasoline, tons
Quarter 1
Quarter 2
Quarter 3
Quarter 4
25 641.03
25 925.93
26 210.83
22 222.22
COMPANY ACTIVITY RESULTS, RUB
Year 1
Year 2
Year 3-4
Year 5-7
Revenue
0
2 837 170 678
5 674 341 356
8 511 512 034
Expenses
0
-1 583 229 237
-3 132 246 854
-4 551 427 230
Net Income
0
1 253 941 441
2 542 094 502
3 960 084 804
7. TECHNOLOGICAL PROCESS BRIEF DESCRIPTION
The raw material which goes to reactor is associated oil gas or natural gas containing methane, ethane, propane, butane and other
components. The process may be realized at pressure from 1.5 to 500 at.
Oxygen for reactor is received from air by the method of electromembrane separation with its further special preparation to
facilitate the reaction.
The process of alcohols synthesis is implemented with heat liberation. The optimum temperature for this process is 200-270oС.
Chemical reaction of alcohols synthesis:
1. 2CH4+O2=2CH3OH
from 1m3 of methane
→
1.43 kg of methanol is produced
2. 2C2H6+O2=2C2H5OH
from 1m3 of ethane
→
2.05 kg of ethanol are produced
3. 2C3H8+O2=2C3H7OH
from 1m3 of propane
→
2.68 kg of propanol are produced
4. 2C4H10+O2=2C4H9OH
from 1m3 of butane
→
3.30 kg of butanol are produced
The produced alcohols are extracted from gas phase in liquid form and are directed to the block of petrol synthesis. Depending on
the demand of a client, any alcohol from the mixture can be extracted as a separate product. The gas fractions which have not
entered into reaction are directed to the block of extraction of helium and hydrogen. The balance of produced alcohols depends
on the content of initial gas.
The synthesis of petrol is realized in isothermal reactor with stationary level of high-silicon zeolite catalyst. Service life of
catalyst is three years. The flow of raw material is heated to the temperature of 300-350oС. Space velocity of feeding alcohols:
0.5-1.5 h. Alcohols conversion index during the reaction is not less than 90-95%. Output of liquid hydrocarbons: 38-45%.
Maximum temperature of the reaction: 430 oС.
8. TECHNOLOGICAL PROCESS ADVANTAGES
1.
The synthesis of alcohols is realized without intermediate stages.
2.
The process is going at any pressure, there is no need in regulating pressure, the
synthesis may be fulfilled from natural gas at high pressure and from associated
gas where the pressure is not high.
3.
It does not demand compressing equipment.
4.
The process may be exercised in the field conditions of oil and gas production.
It permits to implement the cost-effective development of small and middle gas
fields and gas condensate fields, remote and low-pressure fields, fields of shale
gas, gas at sea-based platforms, also to process associated gas directly at oil fields.
9. PLANT GENERAL TECHNOLOGICAL SCHEME FOR BRATSK GAS CONDENSATE FIELD
Oxygen
38 576 791 m3/year
5400 kW
Reactor of
direct synthesis of
alcohols and
oxo compounds
from natural gas
Nitrogen
for consumers
Natural gas
35 000 000 m3/year
Electrochemical
fuel cell
Residual gases:
hydrogen, helium,
carbon dioxide
Alcohols and
oxo compounds
(table 1.1)
Gaseous hydrogen
1 076 288 m3/year
Membrane apparatus
of producing helium
Block of
petrol synthesis
Hydrogen
Helium
97000 m3/year
Petrol
24 000 tons/year
Blowing-off gases (table 1.2)
Membrane
separator of air
Air
Table 1.1
Alcohols and Oxo Compounds
Item
tons/year
СН3ОН
50 975.0
С2Н3ОН
564.0
С2Н5ОН
2 758.0
С3Н5ОН
304.0
С3Н7ОН
1 813.5
i-С4Н9ОН
966.0
n-С4Н9ОН
319.0
С4Н7ОН -2-trans
54.7
С4Н7ОН -2-cis
50.4
Table 1.2
Blowing-off Gases
Item
tons/year
Н2
59.9
СН4
487.6
СО
87.3
СО2
63.3
С2Н4
358.8
С2Н6
115.8
С3Н6
220.1
С3Н8
876.0
i-С4Н10
557.4
n-С4Н10
250.1
i-С4Н8 + С4Н8-1
541.2
С4Н8-2-trans
42.5
С4Н8-2-cis
39.2
13. CATALYST
Catalyst of receiving petrol from methanol of NKT-1 mark.
Possible supplies: “New catalystic technologies” LLC.
Design: extrudate having diameter 3-4 mm of white or yellowish colour.
Composition:
High-silicon zeolite (% of mass)
Promoting agents (% of mass)
Bonding agent (% of mass)
70.0
5.0
25.0
Portion of weight loss during tempering at 550 °С, % mass, not more than
Degree of crystallinity of zeolite, %, not less than
Containing dust and granulate, % of mass, not more than
Density, in filling layer, kg/m3
Strength index, kg/mm of diameter
Conversion of methanol, %, not less than
Output of liquid hydrocarbons, % of mass of source methanol
Temperature of reaction start, oC
Maximum temperature of reaction, oC
Maximum temperature of reactivation, oC
Process pressure, mPas
Space velocity of feeding methanol, h -1
5.0
100
2.0
550-800 (according to producer's data 700-750)
1.5
95
35 ÷ 38
350-360
430
550
0.7÷1.0
0.8÷1.2
Cycle length of catalyst at space velocity 1 h-1 and degree of conversion of
methanol 95%, hour
>500
Service life of catalyst, year, not less than
3
14. MATERIAL AND PRODUCT BALANCE OF PLANT
Flow name
1
Taken:
Raw materials 98% methanol, including
methanol
Recycle of raw methanol, including
methanol
Total:
Produced:
Blowing-off gases, including
of separator
of column
High octane component of petrol
Hydro- methanolic mixture, including
methanol
Total:
Kg per hour
2
Outlet
Thousand t/year*
3
% of mass for raw materials
4
180
176.5
63.5
62
243.5
1.107
1.085
0.39
0.381
1.497
100.0
98.0
35.27
34.44
135.27
15
8
7
60.5
168
62
243.5
0.092
0.049
0.043
0.372
1.033
0.381
1.497
8.33
4.44
3.89
33.61
93.33
34.44
135.27
* number of working hours is taken of 6150
The reactor produces 105 kg/h of water steam of 18 at of absolute pressure due to heat removal.
It wastes for its own needs 10 kg/h of steam (for heating cube of stabilizer).
15. END PRODUCTS CHARACTERISTICS
Gas
with the minimum temperature of burning not less than
molecular mass
density
containing H2
containing С3 -С4
11 400 kcal/kg
20.9
0.885 kg/mn3
to 32% of volume
to 43% of volume
The complete component composition is mentioned in technical documentation.
High octane component of petrol
Density at 15°С
Molecular mass
Containing paraffin hydrocarbons
Containing olefin hydrocarbons
Containing naphthene hydrocarbons
Containing aromatic hydrocarbons
Octane number (RON), not less than
Octane number (MON), not less than
Pressure of saturated steams of petrol, mm, not more than
Fractional composition:
start of distillation temperature, °С
10%
50%
90%
end of boiling temperature, °С
The complete component composition is mentioned in technical documentation.
755 kg/m3
90
38-42% of mass
6-7% of mass
9-11% of mass
30-35% of mass (containing benzol: 0.05 - 0.1% of mass)
92
84
500
35
55
120
160
205