Liquefaction Plant Research Articles

Organization of K60-D strength class sheet rolled stock production intended for electro-welded pipes of pipelines and distribution systems of LNG production plants

A technology of К60-D strength class sheet rolled stock production at 2800 mill of JSC “Ural Steel” elaborated and implemented, by application of thermomechanical rolling followed by accelerated cooling. It was shown that the implemented technology provides the required complex of mechanical properties and high resistance of the rolling stock within a wide dimensional range. The thickness of the rolling stock, produced for trunk pipelines and field oil and gas pipelines, gas-collecting nets pipelines and natural gas liquefaction plants as well as pipelines details was 21.2; 28.5 and up to 45 mm correspondently. Complete meeting the properties of the К60-D strength class sheet rolled stock, produced by the elaborated technology, the requirements to the materials for two-seamed 1420 mm diameter pipes of D category was confirmed by results of tests.

Hydraulic Design of Thermally Coupled Columns and a DWC for NGL Fractionation Plants

Combining a conventional demethanizer with thermally coupled deethanizer and propane-butane recovery columns or a three-product dividing wall column (DWC) provides a realistic opportunity for natural gas liquids (NGL) fractionation complexes as encountered in floating, as well as on-land natural gas liquefaction plants, to minimize energy requirements and reduce carbon dioxide emissions accordingly, in a cost-effective way. The present paper addresses and discusses hydraulic design aspects of these two thermal coupling arrangements, including the choice of the most appropriate column internals that largely depends on important design, construction, and operating considerations that differ for floating and on-land plants.

Тенденции территориальной организации промышленности в постсоветской России и их потенциальные экологические последствия

The trends of the territorial organization of industry associated with new construction in post-Soviet Russia have been determined. An exceptional territorial differentiation of industrial construction is revealed, which implies primarily its overconcentration in Moscow oblast as well as in the north- west (St. Petersburg and Leningrad region). The northern and eastern regions of the country are characterized by focal industrial development and the dominance of mining enterprises. In Asian Russia, large-scale industrial construction is allocated to Kuzbass, and Yamalo-Nenets and Khanty-Mansi Autonomous Okrugs, but the “density” of development is small. In the course of market reforms, the total fragmentation of a single national economic complex was replaced by an unstable trend of the spontaneous formation of complexes. The new economic conditions saw the emergence of new sectors and production facilities: development of oil and gas resources on the shelf of the Sea of Okhotsk and the Caspian, Baltic, Pechora and Black Seas; gas liquefaction plants, and automobile assembly enterprises. Analysis of the structure of the new industrial construction did not reveal any signs of its ecologization. Two thirds of the new facilities refer to basic, environmentally “aggressive” sectors. The ever-increasing concentration of the industry in the few areas of economic activities is the main thrust of territorial development of Russia. Emerging in the vicissitudes of the market, it is negative from the ecological as well as geopolitical standpoint.

Использование возобновляемых источников энергии и установок ожижения природного газа на газораспределительных станциях

Использование возобновляемых источников энергии и установок ожижения природного газа на газораспределительных станциях

Integration of fault tree and importance measure for toxic prevention barrier

This paper discusses the procedure of integrating importance measures into fault tree analysis. Importance measures (IM) are analytical tools developed to quantitatively appraise the contribution of a plant component towards the overall risk. As part of safety assessment, this method can be used to rank and identify the root cause of undesired events. The critical component is usually prioritised in order to improve the reliability of the system. Fussell-Vesely (FV) importance measure is one of the most commonly used IM. This method is applied to a case study involving typical toxic prevention barriers based on an LNG liquefaction plant. This paper also includes event ranking using other IM.

ANN-based correlation for frictional pressure drop of non-azeotropic mixtures during cryogenic forced boiling

A crucial aspect of Joule-Thomson cryocooler analysis and optimization is the accurate estimation of frictional pressure drop. This paper presents a pressure drop model for boiling of non-azeotropic mixtures of nitrogen with hydrocarbons (e.g., methane, ethane, and propane) in microchannels. These refrigerant mixtures are important for their applicability in natural gas liquefaction plants. The pressure drop model is based on computational intelligence techniques, and its performance is evaluated with the mean relative error (mre), and compared with three correlations previously selected as most accurate: Awad and Muzychka; Sun and Mishima; and Cicchitti et al.Comparison between the proposed artificial neural network (ANN) model and the three correlations shows the advantages of the ANN to predict pressure drop for non-azeotropic mixtures. Existing correlations predict experimental data within mre = 23.9–25.3%, while the ANN has mre = 8.3%. Additional features of the ANN model include: (1) applicability to laminar, transitional and turbulent flow, and (2) demonstrated applicability to experiments not used in the training process. Therefore, the ANN model is recommended for predicting pressure drop due to accuracy and ease of applicability.

Simulation of boil-off losses during transfer at a LH2 based hydrogen refueling station

Losses along the LH2 pathway are intrinsic to the utilization of a cryogenic fluid. They occur when the fluid is transferred between 2 vessels (liquefaction plant to trailer, trailer to station storage, station storage to pump or compressor, then possibly onto fuel cell electric vehicles …) and when it is warmed up due to heat transfer with the environment. Those losses can be estimated with good accuracy using thermodynamic models based on the conservation of mass and energy, provided that the thermodynamic states are correctly described. Indeed, the fluid undergoes various changes as it moves along the entire pathway (2 phase transition, sub-cooled liquid phase, super-heated warming, non-uniform temperature distributions across the saturation film) and accurate equations of state and 2 phase behavior implementations are essential. The balances of mass and energy during the various dynamics processes then enable to quantify the boil-off losses. In this work, a MATLAB code previously developed by NASA to simulate rocket loading is used as the basis for a LH2 transfer model. This code implements complex physical phenomena such as the competition between condensation and evaporation and the convection vs. conduction heat transfer as a function of the relative temperatures on both sides of the saturated film. The original code was modified to consider real gas equations of state, and some semi-empirical relationships, such as between the heat of vaporization and the critical temperature, were replaced by a REFPROP equivalent expression, assumed to be more accurate. Non-constant liquid temperature equations were added to simulate sub-cooled conditions. The model shows that under environmental heat transfer only the liquid phase of a LH2 vessel would experience cooling, while the boil-off is mainly a result of evaporation from the saturation film onto the vapor phase. Under the conditions assumed for this work, it was also concluded that the actual LH2 density was lower than the corresponding saturation density given by the working pressure of the vessel. During a bottom fill transfer, for example from a LH2 trailer to an on-site stationary vessel, it is shown that the boil-off losses are due to the compression of the vapor phase (“pdV” force). The model indicates that the magnitude of those losses is not dependent on the regulated pressure in the receiving vessel but is rather a function of the initial pressure in the vessel, amounting to more than 12% of losses for a vessel initially at 100 psia. At last, the model is used to estimate the amount of vapor H2 vented when depressurizing a LH2 trailer following a LH2 delivery.

Conceptual design and analysis of a novel process for hydrogen liquefaction assisted by absorption precooling system

Hydrogen liquefaction processes have effective function in the hydrogen supply chain. However low efficiency and high liquefaction costs are still the most important concerns about the liquefaction plants. In this study a new configuration for a hydrogen liquefier process is proposed and energy-exergy analyzed. The production rate of the liquid hydrogen (LH2) is 90 tons per day that can supply the required LH2 of at least 90 k-180 k hydrogen vehicles in an urban area that results in the reduction of pollutions caused by carbon dioxide emission. The process is simulated in Aspen HYSYS simulator. In addition, it is optimized thorough a trial and error approach that is a functional and simple method of complicated systems analysis. The process includes a mixed refrigerant (MR) refrigeration cycle that precools feed gas hydrogen from 25°C temperature to −199.9°C temperature. A new MR is used in a cascade Joule-Brayton cycle that deep-cools the low-temperature gaseous hydrogen from −199.9°C temperature to −252.2°C temperature in the cryogenic section of the plant. The novel process involves also an absorption refrigeration system (ARS) that cools some hydrogen streams in the precooling and cryogenic sections of the process. The consumed energy per kilogram of produced LH2 is achieved as 6.47kWh. This quantity is 2.89kWh in the ideal conditions. The exergy efficiency of the plant is evaluated to be 45.5% that is significantly more than the exergy efficiency of the in operating hydrogen liquefiers in the world. The energy analysis reveals that the coefficient of performance (COP) of the overall system is 0.2034. The achieved COP is a higher amount in compare to the other similar processes. A sensitivity analysis is done to show the effect of the various operation conditions of the process on the features of the plant. Accordingly, the optimum mass flow of the ARS is determined as 207kg/s for the proposed configuration. As well as, the effect of the change in the temperature approach of the heat exchangers and the changes in the adiabatic efficiency of the compressors and expanders on the SEC, COP, and the exergy efficiency of the overall plant is discussed. Furthermore, financial analysis of the plant estimates the capital expenditures (CAPEX), energy expenditures (EEX), and operational and maintenance expenditures (OMEX) as 25413 €2000, 7370 €2000, and 2033 €2000 respectively. These can be specially improved be improving of the exergy efficiency of the plant. The results implicates that the proposed configuration has better performance indicators than the in-service liquefiers. Therefore, LHL plant manufacturer can be considered it in the design and development of new plants. As well as, researchers may utilize its operating conditions to improve the proposed processes.

Real-Time Synthetic Conversion of the Entire Flared Associated Natural Gas Stream to Liquefied Petroleum Gas (LPG)

About 1,000 scf of gas is produced with every barrel of oil produced in Nigeria which implies that about 2.8 billion scf of associated gas is produced daily, based on the OPEC allowed 2.8 million barrels per day (bpd). At present, about 50% of the associated stranded natural gas produced in Nigeria is still being flared, that is 1.4 billion scf (30,960.974 tons or 30,960,974 kg of LPG equivalent on conversion)daily. On the other hand, Nigeria's annual consumption of LPG is expected to be 2.0 million metric tons this 2018 while 11.3 million metric tons (30,960.974 x365 tons =11,300,755.51 tons or 11,300,755,510 kg) can be produced annually from the entire flared gas. The major components of LPG (propane and butanes) hydrocarbons are gaseous at normal atmospheric temperature (200C) and pressure (14.7psia, 0psig), but are readily liquefied through pressurization (by compression) at relatively moderate pressures less than 200psig at room temperature (250C), leading to volume reduction from 270 scf of gas to 1 cubic feet of liquid, which implies that the flared 1.4 billion scf in gaseous form will reduce to approximately 5.2 million cubic feet in liquid form. The investigation on the real-time Synthetic Conversion of the Entire Flared Association Gas Stream to liquefied Petroleum Gas (LPG) is focused on the use of customized skid mounted mini gas liquefaction plants aimed at cracking the C5+ fractions to the lighter molecules of C3 and C4 as well as steam reforming the C1 and C2 fractions to the heavier molecules of C3 and C4. The approach is based on the fact that it is technically feasible to synthesize almost any hydrocarbon from any other using chemical transformation operations to change the proportions of the hydrocarbons contents. The actual hydrocarbons percentage in typical flare line is 97.61%, and for the 20 million scfd flare stream it is equivalent to 19,522,000 scfd, that is 442.300 tons or 442,300 kg of LPG daily. Assuming that 20 % of the chemical energy of the entire flare stream is released as heat energy in the process, it implies that 80 % of the hydrocarbon component of the flare stream is available for conversion to LPG daily i.e. (442,300 x 0.8) = 353,840 kg. Annually it is equivalent to 442.300 x 365 tons (161,439.5 tons or 161,439,500 kg). Currently there are about 350 bottling plants while to saturate the market with LPG the country needs about 2000 bottling plants. The LPG producible from the countries flared stranded gas, will be is sufficient to saturate the Nigerian market with LPG, drastically reducing the retail price of LPG that is presently hinged on the NLNG international market fundamentals as well as improve on Nigeria's per capita usage of LPG which is currently ranked the lowest in Sub-Saharan Africa. LPG is a group of flammable hydrocarbon gases that are commonly used as fuel in heating appliance, cooking equipment, vehicles, as well as for refrigerant, aerosol propellants and petrochemical feedstock. Although each of the specifications of LPG (commercial propane, commercial butane, is o butane, mixture of propane- butane) have some areas of preference, based on their different physical properties, any device that is suitable for any of the LPG category, would also be suitable for the others, primarily by adjustments on the maximum flow rate, to adopt to the maximum output of the device. Due to the strong quest for cleaner energy and numerous petrochemical/chemical products from methane, ethane, propane and butanes, the world is presently witnessing rapid transition from the "gasoline age" to what might be called "LPG/methane age or methane economy".

Surrogate-assisted modeling and optimization of a natural-gas liquefaction plant

In this study, surrogate-assisted modeling and optimization of the single mixed refrigerant process of natural-gas liquefaction is presented. The mixed refrigerant liquefaction process is highly nonlinear owing to the involved thermodynamics that increase the computational burden of any optimization algorithm. To address the computational-burden issue and obtain the results in a reasonable time for the complex single mixed refrigerant process, an approximate surrogate model was developed using a radial basis function combined with a thin-plate spline approach. Even with the reduced model, all the results obtained were comparable with those by rigorous first-principle models. This confirms that all the important characteristics of the model are correctly captured, and the surrogate models of the liquefaction plant are acceptable replacements of first-principle models, especially in computationally demanding situations.

Thermo-economic analysis of a natural gas liquefaction plant

Increasing worldwide energy demand requires the replacement of fossil fuel sources with clean and alternative ones to limit the chances of a climate collapse. In this scenario, natural gas supplies approximately 30% of total energy demand and is forecasted to become increasingly important in the near future. SOx emission limits for maritime transportation redefined by the International Maritime Organization (IMO) and the implementation of the European Directive for Alternative Fuels Infrastructure (DAFI) are going to produce a fast growth in LNG consumption in the coming decades. A thermo-economic analysis of a natural gas liquefaction plant has been conducted. The scheme is a simplified version of ConocoPhillips Optimized Cascade process that takes into account all principal components such as compressors, heat exchangers, after coolers and storage tanks. The aim of this paper is firstly a thermodynamic analysis of a three-pressure levels plant and, secondly, an economic evaluation of the solution, in order to compare the cost of LNG produced with its price on the market. In the end, sensibility analyses have been executed to consider market price variations and estimation errors concerning assumptions made.

Improved Configurations For Liquefied Natural Gas Cycles

The most important challenge in a natural gas liquefaction plant is to improve the plant energy efficiency. A process topology should be implemented, which results in a considerable reduction of energy consumption as the natural gas liquefaction process consumes a large amount of energy. In particular, system design focusing on configuring cold part cycle is an attractive option. In this study, various energy recovery-oriented process configurations and the potential improvements of energy savings for small- & midscale liquefied natural gas plants were proposed and compared with almost exclusively commercial trademarks processes. These improved simulation based investigations were validated under the variation in feed gas pressure, mixed refrigerant cooling reference temperature and the pinch temperature of cryogenic plate fin heat exchanger. The simulation results exhibited considerable reduction of specific total energy consumption. Therefore, the proposed liquefaction cycles have a simple topology, hence lower capital cost and compacter plant layout, which is compatible for power-efficient, offshore, floating liquefied natural gas liquefaction plants.

Numerical study on the condensation flow and heat transfer characteristics of hydrocarbon mixtures inside the tubes of liquefied natural gas coil-wound heat exchangers

Coil-wound heat exchangers (CWHEs) have been widely used in natural gas liquefaction plants nowadays. But few studies on the condensation heat transfer and frictional pressure drop of mixed hydrocarbon refrigerants inside the tubes of CWHEs have been conducted under practical conditions. In this study, numerical simulations were carried out to investigate the condensation flow and heat transfer characteristics of mixed hydrocarbon refrigerants inside the tubes of liquefied natural gas (LNG) CWHEs under practical operating conditions. A combinational numerical method based on computational fluid dynamics (CFD) simulation and modified Silver method was proposed to predict the condensation heat transfer coefficients of mixtures. The numerical results showed good agreement with experimental data and calculation results by the empirical correlation in the literature. The relative errors of void fraction, heat transfer coefficient and frictional pressure drop were predicted within ±5%, ±15% and ±15% respectively. The simulation results indicated that the heat transfer coefficients of mixed refrigerants varied slightly with the increase of vapor quality, but significantly with the increase of mass flux. And the frictional pressure drop increased with the increase of both vapor quality and mass flux. This study is instructive to the design and optimization of CWHEs used for natural gas liquefaction process.

Influence of component proportion on heat transfer characteristics of ethane/propane mixture flow condensation in shell side of helically baffled shell-and-tube heat exchanger

The component proportion of ethane/propane mixture varies during the condensation process in shell side of helically baffled shell-and-tube heat exchangers of nature gas liquefaction plants, which significantly influences the heat transfer characteristics. In the present study, the heat transfer coefficients of ethane/propane mixtures with ethane mass fraction of 8–50% (covering practical conditions) were tested, and were compared with those of pure propane (0% ethane mass fraction) to analyze the influence of component proportion. The research results indicate that, the maximum heat transfer coefficient of ethane/propane mixture occurs at vapor quality around 0.8; as the ethane mass fraction increases from 0% to 15%, the heat transfer coefficient decreases dramatically by a maximum of 66.3%; as the ethane mass fraction further increases from 15% to 50%, the heat transfer coefficient keeps almost constant, and the fluctuation is within −26.4% to 29.1%. A new heat transfer correlation has been developed, and its prediction deviations are within ±25%.

Off-design performance of a liquefied natural gas plant with an axial turbine of novel endwall design

A design optimization workflow for the casing of a 1.5 stage axial turbine is implemented through a novel endwall surface definition, towards improving the turbine efficiency. The new non-axisymmetric casing design compares favourably to an established diffusion design technique. The workflow uses an axial turbine three-dimensional Reynolds Averaged Navier-Stokes model built in OpenFOAM Extend 3.2 with the k-ω Shear Stress Transport turbulence closure. Computer-based optimization of the surface topology using a Kriging surrogate model automates the design process. The designs are optimized using the total pressure loss across the full stage as the target function. Axial turbine performance gains are obtained from the workflow, which persist both at the design condition and off-design. These gains are used to project the impact of equivalent design improvements to the power turbine of a representative Natural Gas liquefaction plant cycle. Cycle Coefficient of Performance enhancements between 2.05% and 2.923% are obtained, at design and at off design conditions. Implementing these performance improvements has the potential to reduce carbon dioxide emissions by 165.54 tonnes per year at design and by 108.18 tonnes per year at off design, in a representative Natural Gas liquefaction plant.

Self-optimizing control of an LNG liquefaction plant

In this paper we apply self-optimizing control (SOC) to a cascaded LNG liquefaction plant. We first introduce the model, and then define the operational objective, which is to achieve minimal energy consumption while satisfying operational constraints. Four control structures are compared; a “standard” temperature control structure, an SOC structure with two plant measurements, an SOC structure that uses a combination of plant measurements as controlled variable, and an SOC structure where we also include measurements of disturbances in addition to the plant measurements. We find that the SOC structures significantly reduce the average steady-state loss when the operating conditions change. We furthermore find that using more plant measurements in the SOC structure results in lowered losses. In particular, for the disturbances considered, the steady-state loss becomes acceptably low, such that there is no need for a supervisory real-time optimization layer. Finally, it has been found that including disturbance measurements results in somewhat reduced losses, although the improvement was insignificant for the studied case. The effectiveness of the SOC framework is shown by closed-loop step responses to selected disturbances.

Reducing the exergy destruction in the cryogenic heat exchangers of hydrogen liquefaction processes

A present key barrier for implementing large-scale hydrogen liquefaction plants is their high power consumption. The cryogenic heat exchangers are responsible for a significant part of the exergy destruction in these plants and we evaluate in this work strategies to increase their efficiency. A detailed model of a plate-fin heat exchanger is presented that incorporates the geometry of the heat exchanger, nonequilibrium ortho-para conversion and correlations to account for the pressure drop and heat transfer coefficients due to possible boiling/condensation of the refrigerant at the lowest temperatures. Based on available experimental data, a correlation for the ortho-para conversion kinetics is developed, which reproduces available experimental data with an average deviation of 2.2%. In a plate-fin heat exchanger that is used to cool the hydrogen from 47.8 K to 29.3 K with hydrogen as refrigerant, we find that the two main sources of exergy destruction are thermal gradients and ortho-para hydrogen conversion, being responsible for 69% and 29% of the exergy destruction respectively. A route to reduce the exergy destruction from the ortho-para hydrogen conversion is to use a more efficient catalyst, where we find that a doubling of the catalytic activity in comparison to ferric-oxide, as demonstrated by nickel oxide-silica catalyst, reduces the exergy destruction by 9%. A possible route to reduce the exergy destruction from thermal gradients is to employ an evaporating mixture of helium and neon at the cold-side of the heat exchanger, which reduces the exergy destruction by 7%. We find that a combination of hydrogen and helium-neon as refrigerants at high and low temperatures respectively, enables a reduction of the exergy destruction by 35%. A combination of both improved catalyst and the use of hydrogen and helium-neon as refrigerants gives the possibility to reduce the exergy destruction in the cryogenic heat exchangers by 43%. The limited efficiency of the ortho-para catalyst represents a barrier for further improvement of the efficiency.

Global cost optimization of a mini-scale liquefied natural gas plant

Cryogenic natural gas liquefaction plant has huge capital and operating expenses corresponding to operating equipment and energy utilization. Considering ever-increasing energy price, therefore, minimization of energy consumption rate for a better profit is highly required. However, any un-engineered energy cut off would result in larger surface area of heat-exchanger and hence bigger capital cost. Here, the net profit of establishing a mini 50 ton/day liquefied natural gas facility, operating for 25 years, is optimized via Genetic Algorithm technique. Poly Refrigerant Integrated Cycle Operations (PRICO) process is simulated in HYSYS environment and linked to MATLAB software for subsequent maximization. The simulation resulted in total consumed power, heat exchanger area and total profit by 2745.33 kW, 3285.58 m2 and 1266.64 million$, respectively. In order to determine unit efficiency and plant irreversibility rate, exergy analysis is performed on individual equipment. Basically, thirteen independent variables are considered for optimization of objective function. Sensitivity analysis for objective function is considered by altering each variable. Final results indicate 9.26% rise in total profit (1383.95 million$) by 59% reduction in energy utilization (1127.68 kW) and 37.50% in heat-exchanger size (2053.7 m2). Meanwhile, the total and heat-exchanger exergy losses are decreased by 65.8% and 80.7%, respectively.

Industrial and Transport Development of the Territory of Russia in the Post-Soviet Period

The inventory of implemented investment projects was used as the basis for compiling a smallscale map to display the main features of industrial and transport development of the territory of post-Soviet Russia. An exceptional territorial differentiation of industrial construction is revealed, which implies primarily its overconcentration in Moscow oblast as well as in the north-west (St. Petersburg and Leningrad oblast). The northern and eastern regions of the country are characterized by focal industrial development and the dominance of mining enterprises. In Asian Russia, large-scale industrial construction is allocated to Kuzbass, and Yamalo-Nenets and Khanty-Mansi Autonomous Okrugs, but the “density” of development is small. In many areas, new enterprises are similar in their specialization to the economic profile of a given area. Signs of territorial-production integration of enterprises in the specific conditions of the Russian market are identified. The new economic conditions saw the emergence of new sectors and production facilities: development of oil and gas resources on the shelf of the Sea of Okhotsk and the Caspian, Baltic, Pechora and Black Seas; gas liquefaction plants, and automobile assembly enterprises. Only a quarter of the new industrial enterprises are located in regional capitals. The dispersion of industries within separate regions is determined by the high proportion of extractive enterprises, the formation of special economic zones outside the regional centers, and by the low cost of land and labor in small towns and villages. The new “village” industry has a broad spectrum of specialization and is not limited to processing agricultural raw materials. Analysis of the structure of the new industrial construction did not reveal any signs of its ecologization. Two thirds of the new facilities refer to basic, environmentally “aggressive” sectors. Most of the newly built transport infrastructure facilities are specialized in satisfying the export requirements of the country’s economy, rather than in enhancing connectivity of its territory. Intensive construction of ports and pipelines leads to the concentration of anthropogenic pressure on the water areas and the coasts, in particular the Baltic, Black and Azov Seas. The resulting map reveals new foci and areas of change in the natural environment and its large-scale transformation.

Hydrogen transfer during co-liquefaction of Elbistan lignite and biomass: liquid product characterization approach

ABSTRACTIn this study, Elbistan lignite (EL) and manure were liquefied under catalytic conditions in an inert atmosphere. Red mud, tetralin, and distilled water were used as a catalyst and solvent, respectively. The liquefaction studies were carried out under catalytic conditions in the catalyst concentration of 9%, solvent/solid ratio of 3/1, reaction time of 60 min, waste/lignite ratio of 1/3, and at temperature of 400°C. Stirring speed and initial nitrogen pressure were kept constant at 400 rpm and 20 bar, respectively. At the end of liquefaction process, the soluble liquefaction products were separated by successive solvent extraction to preasphaltene, asphaltene, and oils. Oil products characterized by H-NMR to be able to differ hydrogen transfer from manure to EL surface. To obtain the hydrogen transfer way, liquefaction experiments conducted under inert atmosphere which does not related to hydrogen reaction, other above experimental conditions were kept same but only solvent type changed. The reason of using distilled water instead of tetraline is tetraline known as hydrogen donor but not water. Because water behaves supercritical conditions during the liquefaction stage. EL liquefied alone while using tetraline however EL liquefied with manure with using distilled water as a solvent. The obtained oil products form both experiments characterized by H-NMR. The radical groups diffraction and range values are not changed significantly shows that manure behaved as an hydrogen donor. So, EL with manure is the one great option to reduce cost of hydrogen source for direct coal liquefaction plant.