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DALLAS--(BUSINESS WIRE)--Flowserve Corporation (NYSE: FLS), a leading provider of flow control products and services for global infrastructure markets, today announced an order close to $80 million to provide pumps and ebulators for the Hengli Integrated Refining Complex Project, a 400,000 barrel-per-day final conversion refinery on Changxing Island in Dalian, Liaoning Province in China. The order includes nearly 200 pumps, which will be used in an integrated refining and petrochemical project for the Hengli Petrochemical Complex. Flowserve will work in coordination with SINOPEC Luoyang Petrochemical Engineering Corporation (LPEC). “ A project of this size requires an ongoing supply of reliable, high-quality equipment to enable full and successful operation,” said Kim Jackson, President, Flowserve Engineered Product Operations. “ Our team is committed to meeting demands on this scale, and our geographic accessibility and extensive experience with orders of this magnitude make us well equipped to do so.” The Flowserve products will be sourced primarily from its facilities in Vernon, USA; Desio, Italy; and Suzhou, China, with phased deliveries beginning in early 2018 to support the project as it moves forward. In addition to the original equipment award, additional aftermarket awards will exist from this order. About Flowserve: Flowserve Corp. is one of the world’s leading providers of fluid motion and control products and services. Operating in more than 55 countries, the company produces engineered and industrial pumps, seals and valves as well as a range of related flow management services. More information about Flowserve can be obtained by visiting the company’s Web site at www.flowserve.com. Safe Harbor Statement: This news release includes forward-looking statements within the meaning of Section 27A of the Securities Act of 1933 and Section 21E of the Securities Exchange Act of 1934, which are made pursuant to the safe harbor provisions of the Private Securities Litigation Reform Act of 1995, as amended. Words or phrases such as "may," "should," "expects," "could," "intends," "plans," "anticipates," "estimates," "believes," "forecasts," "predicts" or other similar expressions are intended to identify forward-looking statements, which include, without limitation, earnings forecasts, statements relating to our business strategy and statements of expectations, beliefs, future plans and strategies and anticipated developments concerning our industry, business, operations and financial performance and condition. The forward-looking statements included in this news release are based on our current expectations, projections, estimates and assumptions. These statements are only predictions, not guarantees. Such forward-looking statements are subject to numerous risks and uncertainties that are difficult to predict. These risks and uncertainties may cause actual results to differ materially from what is forecast in such forward-looking statements, and include, without limitation, the following: a portion of our bookings may not lead to completed sales, and our ability to convert bookings into revenues at acceptable profit margins; changes in global economic conditions and the potential for unexpected cancellations or delays of customer orders in our reported backlog; our dependence on our customers’ ability to make required capital investment and maintenance expenditures; risks associated with cost overruns on fixed-fee projects and in taking customer orders for large complex custom engineered products; the substantial dependence of our sales on the success of the oil and gas, chemical, power generation and water management industries; the adverse impact of volatile raw materials prices on our products and operating margins; our ability to execute and realize the expected financial benefits from our strategic manufacturing optimization and realignment initiatives; economic, political and other risks associated with our international operations, including military actions or trade embargoes that could affect customer markets, particularly Middle Eastern markets and global oil and gas producers, and non-compliance with U.S. export/re-export control, foreign corrupt practice laws, economic sanctions and import laws and regulations; increased aging and slower collection of receivables, particularly in Latin America and other emerging markets; our exposure to fluctuations in foreign currency exchange rates, including in hyperinflationary countries such as Venezuela; our furnishing of products and services to nuclear power plant facilities and other critical processes; potential adverse consequences resulting from litigation to which we are a party, such as litigation involving asbestos-containing material claims; a foreign government investigation regarding our participation in the United Nations Oil-for-Food Program; expectations regarding acquisitions and the integration of acquired businesses; our ability to anticipate and manage cybersecurity risk, including the risk of potential business disruptions or financial losses; our relative geographical profitability and its impact on our utilization of deferred tax assets, including foreign tax credits; the potential adverse impact of an impairment in the carrying value of goodwill or other intangible assets; our dependence upon third-party suppliers whose failure to perform timely could adversely affect our business operations; the highly competitive nature of the markets in which we operate; environmental compliance costs and liabilities; potential work stoppages and other labor matters; our inability to protect our intellectual property in the U.S., as well as in foreign countries; obligations under our defined benefit pension plans; and other factors described from time to time in our filings with the Securities and Exchange Commission. All forward-looking statements included in this news release are based on information available to us on the date hereof, and we assume no obligation to update any forward-looking statement.

Luoyang Petrochemical Engineering Corporation and Sinopec | Date: 2013-03-29

A fired heater includes a fired heater body with an air inlet and a flue gas outlet, and a flue gas waste heat recovery system communicated with the fired heater body and including at least two heat exchange chambers. A first port of each of the heat exchange chambers can be communicated with the flue gas outlet or the air inlet, and a second port of each of the heat exchange chambers can be communicated with the outside air or a fume extractor. When the first port of at least one heat exchanger chamber is communicated with the flue gas outlet and the second port thereof is communicated with the fume extractor, the first port of at least another heat exchange chamber is communicated with the air inlet and the second port thereof is communicated with the outside air.

Li Q.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2012

As the size of spherical tanks becomes increasingly larger, the steel material requirement and the dimensions of tank pedal plates have become increasingly bigger, which results in a number of difficulties in petal plate forming, transportation, side lifting installation and welding, etc. It is necessary to design the spherical tanks based upon analysis design methods under the conditions of higher requirements in intrinsic safety of spherical tanks' construction and load. The integral stress calculations have been made for 4 loads of different load combination tanks and 2 structures. The force exerting on the spherical tanks at different loads are studied and stresses at the connections between supports and tanks are analyzed. It is concluded that, all stresses should be calculated based upon all possible loads combination, the central model and bestraddle model should be established for load calculation, the maximum stress should be at the connection between support and tank smooth transition should adopted and hexahedral element analysis should be applied for finite element analysis.

Li W.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2013

The sources and forms of sulfur in MTBE are introduced. The sulfur concentration in LPG fractionation unit and MTBE unit are analyzed and concentration cycle concept is presented. When FCC gasoline, reformate and MTBE are the blending components of gasoline, the blending ratio of reformate to MTBE shall be 2. 1/1 ∼5. 3/1 to meet the 10 μg/g mass percentage of sulfur in blending gasoline. Based upon the gasoline quantity and quality of a refinery in China, the blending of Guo V 95 gasoline is simulated using PIMS computer program. The addition of MTBE and addition of reformate of different sulfur mass percentages are calculated. When the sulfur mass percentage of MTBE is the same as that of objective sulfur mass percentage of FCC gasoline and Guo V gasoline, the MTBE addition is maximum, the blending is the most flexible and economic benefits is the highest. The addition of reformate increases with increase of sulfur mass percentage of MTBE, and addition of MTBE is gradually minimized (1.5%). The controlled objective sulfur mass percentage of MTBE is affected by the sulfur mass percentage of FCC gasoline. When the minimum MTBE addition is 8%, the sulfur mass percentage of gasoline is lowered to 8 μg/g from 10 μg/g, and the controlled objective sulfur mass percentage of MTBE increased to 30 μg/g from 12 μg/g. Whereas, reducing the sulfur mass percentage of FCC gasoline may reduce the octane number of gasoline. The optimization of MTBE feedstocks and optimization of operation of desulfurization unit can reduce the sulfur mass percentage in MTBE to 15 ∼60 μg/g-The application of distillation of MTBE product and distillation of C4s feedstock can lower the sulfur in MTBE to 10 μg/g. The comparison has found that the distillation of MTBE product is superior over distillation of C4s feedstock.

Jinfeng Z.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2015

The C4+ charge gas piping is one of the key pipes of DMTO- II unit (the second generation of Dalian Methanol to Olefin Process) , and the spool from C4 + reactor to C4 + quench/water wash tower is the most critical part. The design criteria of the piping are presented for the world' s first large commercial DMTO- II unit whose piping is large in diameter and pipeline media are toxic, inflammable and explosive and containing small amount of catalysts. The following issues are discussed for the C4+ reaction gas piping design-. 1 ) the piping layout; 2) the piping main component's design, including selection of combination of cold wall and hot wall construction, selection of material, calculation of wall thickness, thickness design of heat-insulation and wear-resistant lining in the cold wall piping; 3) the piping flexibility design, including thermal compensation mode, stress analysis, stress check, the selection of structure and material for metal bellows expansion joint; 4) the pipe support and hanger design, including the design criteria of rigid and spring supports and hangers.

Qin K.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2015

The supporting design of the regenerated catalyst standpipe was analyzed. The selection of the support disc spring was studied in detail including calculating the wall temperature, and the thermal expansion of different sections of the Reactor and Regenerator system and how to select support disc spring. The stresses of two ends of standpipe before and after installation of the disc spring have been compared. The stresses of the support disc spring before and after expansiou joint had less 79% than no support disc spring. At the same time, the structure of lining of standpipe was analyzed. The construction of the lining of regenerator standpipe should be designed in consideration of not only thermal insulation but also anti-wearing. The measures to ensure the quality of lining were proposed. After optimization of the design of regenerated catalyst standpipe, the unit has been running for 2 years without trouble of the standpipe. No vibration and overheating of the standpipe have ever occurred. It provides an effective basis for the long-term safe operation of the unit..

Dongxu Z.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2015

The engineering design charaeteristies of feed heater of Vacuum Residue Hydrodesulfurization (VRDS) reactor are described. The impact factors for heat transfer of feed heater of Vacuum Residue Hydrodesulfurization reactor are analyzed by hot zoning simulation method. The study results demonstrate that: CI) when the space between burner and coil is longer, the average heat radiation flux is more uniform. It is suggested the space between tubes should exceed 1.1 m, which can obviously improve uniformity of heat radiation flux of heater; (2)When the burner flame height is higher, the distribution of temperature field inside heater chamber is more uniform. The recommended height should be greater than 30% of the height of chamber, which can significantly improve the uniformity of furnace radiation heat transfer; (3)The adjustment of oil flow direction (adjustment of countercurrent heat transfer for co-current heat transfer) can reduce the peak tube wall temperature and the maximum internal film temperature, which can improve the furnace ability to adapt to the harsh operating conditions.

Wang H.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2015

This paper introduces the status quo of low-temperature waste heat utilization of refineries and the development, technical features and developing trend of low-temperature multi-effect evaporation seawater desalination (LT-MED) process. In a case study of a refinery, the scheme and economy of LT-MED technology for the utilization of waste heat are analyzed and studied. It is concluded that the recovery water temperature in the low-temperature waste heat recovery system of petrochemical company is generally 95 ∼ 100 °C and the heat temperature is generally 65 ∼ 70 °C, which meet the operation requirements of MED; The cost of primary desalted water produced by MED technology is generally 4 ∼ 6 Yuan/m3, and the price of the refinery primary desalted water is generally higher than the 7 Yuan/m3. The construction of MED system based on the desalted water demand will have a good benefit..

Ligong Q.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2015

The fluid catalytic cracking process for maximum iso-hydrocarbon production (MIP) has played an important role in the upgrading of Guo III and Guo IV gasoline, and several MIP processes have been developed. In MIP process, second reaction section is provided which is in series with the riser reactor to make up the spent catalysts for the second reactor section and reduce the hourly space velocity of the second reactor. The mild reaction conditions and intensified isomerization reaction can reduce the olefin in FCC gasoline to less than 35% and benzene to less than 1.0%. Whereas, the MIP-CGP process can reduce the olefin in gasoline to 18% and raise the aromatics in gasoline to over 18%. The octane number of gasoline can be raised by 1 unit and propylene yield can be increased by 8% ∼ 10%. In the MIP-DCR process, a pre-lift mixer is provided for the catalysts, which has greatly lowered the contacting temperature difference of feed oil and catalysts and reduced the dry gas and coke make. The total liquid yield is increased by over 0. 15%. In MIP-LTG process, about 30% light diesel in diesel fraction is returned to riser reactor for further cracking. The LPG + gasoline yield can be increased by over 1.0%, and octane number of gasoline (MON) can be raised by 0. 5 unit.

Liu N.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2015

It is known from analysis of simulation results of a 2. 0 MM TPY hydrocracking unit that the flash points of kerosene and diesel only fluctuate 0 ∼ 2 ∼C when fractionator is flushed by different flowrates (0.5 ∼7 t/h) of steam, hydrogen or nitrogen at the same conditions. These three gases can be used as the fractionator flush medium if only their impact on products flash point is considered. As compared with hydrogen, the use of steam as flush gas for the fractionator bottom can raise fractionator bottom temperature by 18 ∼ 41 °C and reduce the fractionator diameter by 200 ∼ 1 200 mm, which are favorable for heat exchange and the reduction of investment and operation cost of fractionators. As compared with nitrogen, steam has the advantages of minimized impact on product oil storage and transportation and easy recovery and reutilization. Therefore, steam is the most suitable flush medium for fractionators in the three gaseous mediums. In addition, the low-pressure and high superheated temperature (no higher than 425 °C) conditions should be selected for the steam, and its flowrate should be selected in the areas where the initial boiling point of bottom product rises rapidly. In this case, the fractionation precision requirement is achieved, and the unit energy consumption is decreased. Whereas, with the upgrading of product oils and off-specification of water in product oils, effective dehydration equipment, flush medium and process technologies should be developed.

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