2785 results about "Reboiler" patented technology

A process for the recovery of ethane, ethylene, propane, propylene and heavier hydrocarbon components from a hydrocarbon gas stream is disclosed. In recent years, the preferred method of separating a hydrocarbon gas stream generally includes supplying at least portions of the gas stream to a fractionation tower having at least one reboiler, and often one or more side reboilers, to supply heat to the column by withdrawing and heating some of the tower liquids to produce stripping vapors that separate the more volatile components from the desired components. The reboiler and side reboilers (if any) are typically integrated into the feed stream cooling scheme to provide at least a portion of the refrigeration needed to condense the desired components for subsequent fractionation in the distillation column. In the process disclosed, the tower reboiling scheme is modified to use one or more tower liquid distillation streams from a point higher in the column than is used in the conventional reboiling scheme, providing colder stream(s) for the reboiler(s) that allow more effective cooling of the feed streams and thereby improve the efficiency with which the desired components are recovered. In addition, the tower liquid streams withdrawn from a higher point in the column contain larger quantities of the more volatile components, which when vaporized provide better stripping of undesirable components like carbon dioxide without reducing the recovery of the desired components. The heated distillation stream is returned to a lower point on the fractionation tower that is separated from the withdrawal point by at least one theoretical stage.

A process for the recovery of ethane, ethylene, propane, propylene and heavier hydrocarbon components from a hydrocarbon gas stream is disclosed. In recent years, the preferred method of separating a hydrocarbon gas stream generally includes supplying at least portions of the gas stream to a fractionation tower having at least one reboiler, and often one or more side reboilers, to supply heat to the column by withdrawing and heating some of the tower liquids to produce stripping vapors that separate the more volatile components from the desired components. The reboiler and side reboilers (if any) are typically integrated into the feed stream cooling scheme to provide at least a portion of the refrigeration needed to condense the desired components for subsequent fractionation in the distillation column. In the process disclosed, the tower reboiling scheme is modified to use one or more tower liquid distillation streams from a point higher in the column than is used in the conventional reboiling scheme, providing colder stream(s) for the reboiler(s) that allow more effective cooling of the feed streams and thereby improve the efficiency with which the desired components are recovered. In addition, the tower liquid streams withdrawn from a higher point in the column contain larger quantities of the more volatile components, which when vaporized provide better stripping of undesirable components like carbon dioxide without reducing the recovery of the desired components. The heated distillation stream is returned to a lower point on the fractionation tower that is separated from the withdrawal point by at least one theoretical stage.

To provide a method for recovering carbon dioxide, in which thermal energy for regenerating a CO2 absorbing solution and power for compressing the recovered CO2 are supplied, and high thermal efficiency is achieved, and a system therefor. A system for recovering carbon dioxide including a high pressure turbine 3, an intermediate pressure turbine 7, and a low pressure turbine 8; a boiler 1 for generating steam for driving the turbines; an absorption tower 18 filled with a CO2 absorbing solution for absorbing and removing CO2 from combustion exhaust gas of the boiler; a regeneration tower 24 for regenerating the absorbing solution having absorbed CO2; a compressor 42 for compressing the removed CO2; a turbine 41 for a compressor, which is driven by some of the exhaust steam of the high pressure turbine; turbines 51 and 52 for auxiliary machinery, which are driven by some of the exhaust steam of the intermediate pressure turbine; and supply pipes 45 and 55 for supplying exhaust steam of the compressor turbine and the auxiliary machinery turbines to a reboiler 30 of the regeneration tower as a heating source.

The invention relates to a heat exchange system for high temperature heat of a plant, in particular to an oil refining plant high-temperature heat integration system designed for using high-temperature mass flow heat. The system is characterized in that three independent heat source devices are connected through thermal medium pipes and heat-conducting oil in the thermal medium pipes are used as a heat-transfer medium to form heat integration, so as to collect and use high-temperature heat. Compared with the prior art, the system optimizes a heat exchange network, saves fuel gases and steam in a reboiler at the tower bottom, reduces energy consumption of equipment, lowers oil refining cost and improves economic benefits.

The invention relates to an MVR vapor-stripping deamination system. The MVR (Mechanical Vapor Recompression) vapor-stripping deamination system comprises a vapor-stripping deamination tower, an ammonia water rectification tower and a condenser, wherein a high-ammonia-nitrogen sewage input pipe, a vapor input pipe I, a post-deamination waste water discharge port and an ammonia-containing vapor discharge port I are arranged on the vapor-stripping deamination tower; the vapor-stripping deamination tower is connected with a reboiler; the high-ammonia-nitrogen sewage input pipe is connected with waste water feed preheaters (II and I); the post-deamination waste water discharge port is connected with the waste water feed preheater I and an axial flow pump respectively; the ammonia-containing vapor discharge port I is connected with the reboiler through a mechanical vapor compressor; the reboiler is connected with a dilute ammonia water storage tank connected with the ammonia water rectification tower; a discharge port, an ammonia-containing vapor discharge port II and a vapor input pipe are arranged on the ammonia water rectification tower; the discharge port is connected with a rectification tower kettle discharge pump and the waste water feed preheater II; the ammonia-containing vapor discharge port II is connected with the condenser; a strong ammonia water discharge port is connected with a strong ammonia water storage tank connected with the ammonia water rectification tower. Meanwhile, the invention further discloses an application method of the MVR vapor-stripping deamination system. The MVR vapor-stripping deamination system has the advantages of less investment, high feasibility and high comprehensive utilization ration.

A carbon-dioxide-capture-type steam power generation system 1 according to the present invention comprises a boiler 6 producing an exhaust gas 5 by combusting a fuel 2 and having a flue 8; an absorbing unit 40 being configured to absorb the carbon-dioxide contained in the exhaust gas 5 into an absorbing solution; and a regenerating unit 44 being configured to release the carbon dioxide gas from the absorbing solution absorbing the carbon dioxide and discharge the released carbon dioxide gas. Further, in this system, a reboiler 49 is provided for receiving a heating-medium as heat source, producing a steam 43 and supplying the produced steam 43 to the regenerating unit 44. Additionally, in the flue 8 of the boiler 6, a boiler-side heat exchanger 61 is provided for heating the heating-medium by the exhaust gas 5 passing therethrough.

There is disclosed a method and apparatus for treating produced water from a heavy oil thermal recovery unit to achieve water recovery and recycle levels of greater than 80% and as high as 100% to achieve zero discharge criteria. The method includes the initial steps of capturing the waste heat energy from the high pressure steam separator located downstream of the steam generators. Further, transferring the heat energy into a heated separator and reboiler exchanger to distill oil reservoir produced water and recover distilled water and a concentrated brine or solid product. The heated separator concentrated stream is circulated through the reboiler exchanger to maintain from 1% to about 50% mass vapour in the stream returning to the heated separator and prevent fouling and scaling. The apparatus includes a low pressure waste energy separator, heated separator and vapour compressor in combination with a forced circulation circuit to generate the distilled water.

A fully thermally coupled distillation structure designed to overcome hydraulic limitations in the past has been revealed for separating a multi-component feed stream into three product streams. The fractionation apparatus is equipped with at least one condenser and one reboiler to provide fractionation efficiency surpassing the PETLYUK system. Further, the fractionation apparatus includes innovative designs to enable hydraulically balanced and energy efficient operation at various feed rates, compositions and product specifications.

Contemplated configurations and methods include a solvent regenerator (58) that has an upper (93) and a lower stripping section (94). Cooled rich solve is used as reflux while heated rich solvent (11) is used as a source of stripping agent in the upper section (91). A reboiler (62) in the lower section provides further stripping agent, hi especially preferred configurations, a portion of lean solved from the regenerator (58) is further stripped in a separate or integrated regenerator (62) to form an ultra-lean solvent. Both lean and ultra-lean solvents are preferably used in a two-stage absorber (52) to thereby from the rich solvent and an offgas that is very low in acid gas.

The invention discloses an amine liquid desulphurization method with high hydrogen sulphide removal rate and a special device. A regeneration tower is divided into an upper section and a lower section; by a third pipeline which is provided with a third pump and is added between the middle part of an absorption tower and the outlet of the upper section of the regeneration tower, and a fourth pipeline by which the outlet of the regeneration third pump and the inlet of the lower section of the regeneration tower are communicated with each other, two-step absorption and two-step regeneration are carried out by using solvents with different hydrogen sulphide contents, a small part of solvent with little hydrogen sulphide is used as absorbent of final-step, therefore, the solvent quantity which achieves the low content of hydrogen sulphide is little, thus the steam dosage is reduced, the reboiler steam is saved by about 30 percent, the operation energy consumption is greatly reduced and the desulphurization expense is reduced further; meanwhile, the content of the hydrogen sulphide in the processing gas purified by the invention can achieve less than 50ppmv; therefore, the absorption effect is good and the hydrogen sulphide removal rate is high.

The invention discloses a low-pressure ethanol recovery device and method with triple effect rectification. The low-pressure ethanol recovery device with triple effect rectification comprises a first rectifying tower, a second rectifying tower, a third rectifying tower, a rectifying tower reboiler, a rectifying tower feed preheater, a condenser, a return tank, a dilute ethanol feed preheater, a temporary finished product storage tank and a finished product cooler. In the ethanol recovery method with triple effect rectification, by controlling the recovery of the finished ethanol in the second rectifying tower, the content of ethanol in tower bottom wastewater of the second rectifying tower is 5wt%-30wt%, the temperature of the tower bottom wastewater is 100-120 DEG C, and the working pressure of the third rectifying tower is 250-400kPa. The invention adopts the low-pressure triple effect rectification technique and reduces energy loss in the technical process, thus greatly reducing the energy consumption; and the operating pressure and temperature of the third rectifying tower are greatly reduced, and the requirements on the high temperature resistant and corrosion resistant properties of equipment are reduced, thereby reducing the equipment investment and the maintenance cost.

The invention relates to a method for controlling and optimizing the distillation tower. It controls the distillation tower in dependence on the material balance relation and component balance relation, optimizes the distillation tower by using representative model. Employing the abstraction proportion between the light product on the top of the tower and heavy product in the bottom of the tower (in following, taking the proportion between light and heavy product for abbreviation) as main controlled variable depending on the distillation principle, the material balance and component balance in the distillation tower, controlling the proportion between the light and heavy product, temperature, reflux ratio to realize stable operation by regulating the quantity of reflux and heat load of re-boiler. Simulating the practical course through the technological process simulation software, and training the nerve net model to become the representative model for the course optimization. Optimizing the operation with the representative model by using the analytical data for the raw material and product to realize the product Ka bian optimization, increasing the productivity of product with high value on the condition of guaranteeing the product quality and realizing the device energy saving and consumption reduction.

The invention relates to a method for desulphurizing MTBE with high sulphur content, belonging to the field of the refining of methyl tertiary butyl ether (MTBE). The methyl tertiary butyl ether (MTBE) with high sulphur content is placed into a distillation tower and heated by a reboiler, the temperature of a tower kettle is kept between 90 DEG C and 120 DEG C, the pressure of the tower kettle iskept at 0.08+ / -0.02 MPa, the temperature of a tower top is kept between 69 DEG C and 75 DEG C, and the pressure of the tower top is kept at 0.06+ / -0.02 MPa so that a finished product is distilled outof the tower top, a reflux ratio is kept from 1 to 10, and a sulfur product is recycled from a tower bottom. The invention has the advantages of simple process, advanced technology, easy and convenient control operation, little investment, low cost and no three-waste pollution.

A cryogenic process for the production of oxygen by cryogenic distillation using an air separation unit comprising a double column, said double column comprising a high pressure column and a low pressure column comprising the steps of: sending compressed, cooled and purified air to the high pressure column in gaseous form, sending oxygen enriched fluid from the bottom of the high pressure column to the low pressure column, removing nitrogen enriched gas from the top of the high pressure column, sending a first portion of nitrogen enriched gas to a lower reboiler in the low pressure column following compression in a cold compressor having a cryogenic inlet temperature, sending a second portion of nitrogen enriched gas to an upper reboiler in the low pressure column, sending nitrogen enriched liquid from at least one of the first and second reboilers to at least one of the high pressure column and the low pressure column, expanding a stream of nitrogen enriched gas from the high pressure column in an expander following a warming step, driving the cold compressor using a motor and producing oxygen rich gas from the low pressure column by at least one of the steps of removing a gaseous stream and by vaporizing a liquid stream.

A refinery or petrochemical plant may include a fractionation column and related equipment, such as one or more condensers, receivers, reboilers, feed exchangers, and pumps. The equipment may have boundaries or thresholds of operating parameters based on existing limits and / or operating conditions. Illustrative existing limits may include mechanical pressures, temperature limits, hydraulic pressure limits, and operating lives of various components. There may also be relationships between operational parameters related to particular processes. For example, the boundaries on a naphtha reforming reactor inlet temperature may be dependent on a regenerator capacity and hydrogen-to-hydrocarbon ratio, which in turn may be dependent on a recycle compressor capacity. Operational parameters of a final product may be determined based on actual current or historical operation, and implemented in one or more models to determine adjustments for enhanced operational efficiency.

The invention provides a method for controlling an amine solvent regeneration system, belongs to the technical field of amine solvent recovery, and comprises an amine recovery tower. The method is characterized in that a heat supply regulating valve of a tower bottom reboiler is related to system pressure; and a distilled line regulating valve of a tower top product is related to the gas-phase temperature of the tower top. The method can meet the requirement on purification degree of an amine solvent product on the tower bottom only by presetting a system pressure value and a tower top gas-phase temperature vale; and the control system can trace variations of feeding flow rate, feeding quality and feeding temperature to realize automatic regulation and obtain perfect tower bottom products.

The invention relates to a method and a system for preparing high purity gas by a rectification method. According to the method disclosed by the invention, a target gas raw material is firstly processed by a light component removal tower to remove light component impurities and then is processed by a heavy component removal tower to remove heavy component impurities; obtained purified gas is compressed into compressed gas; the compressed gas is at least divided into two parts which are respectively used as heat sources of a tower kettle reboiler of the light component removal tower and a tower kettle reboiler of the heavy component removal tower; the two parts of compressed gas are condensated into liquid to be converged and stored; the stored liquid is divided into three parts; two parts of the stored liquid are respectively used as a cooling medium of a tower top condenser of the light component removal tower and reflux of the heavy component removal tower after being respectively subjected to throttling expansion; and the third part of the stored liquid is recovered as a product. The system disclosed by the invention comprises the light component removal tower, the tower top condenser of the light component removal tower, the heavy component removal tower, a compressor, the tower kettle reboiler of the light component removal tower, the tower kettle reboiler of the heavy component removal tower, a liquid storage tank and a connecting pipeline. The method and the system which are disclosed by the invention have the advantages that equipment is simple; energy is saved; the method and the system are flexible to operate and have wide application; the system is easy to maintain; and the method and the system have few requirements on public works.

The invention relates to a production device and a method of high purity trichlorosilane by using heat pump distillation. Trichlorosilane raw materials enter a de-heavy fractionator to eliminate heavy components after light component elimination through a light component eliminating tower, thereby obtaining high purity trichlorosilane. On the basis, the light component eliminating tower and the de-heavy fractionator both adopt a heat pump distillation process. Cooling medium in a condenser absorbs heat after exchanging the heat with materials on the top of the tower and is evaporated into gas, the gas enters a reboiler as tower reactor heat source reactor liquid after pressure and temperature enhancement through compression, and the gas is condensed into liquid. The liquid returns to the condenser after reduction of expenditure and pressure so as to finish a cycle. Therefore, the heat at the low temperature part of the tower top is transferred to the high temperature part of a tower reactor through the cooling medium. The invention has the advantages that by adopting the heat pump distillation process, the energy consumption can be greatly lowered, and the annual economic benefit is greatly enhanced.

A method for reclaiming CO2 absorbing chemical(s) from a lean aqueous CO2 absorbent leaving a regeneration column (8), where lean absorbent (30) is withdrawn and flashed (31) to generate a vapor that is compressed (34) and returned into the regeneration column as stripper gas (37), where a part of the lean absorbent (20) is withdrawn and introduced into a reclaimer (21) in which the lean absorbent is boiled to generate a gas phase (23) that is withdrawn and returned into the regeneration column as reclaimed absorbent, and a liquid phase containing impurities (24), wherein the gaseous phase that is withdrawn from the reclaimer is compressed (34) together with the vapor part (33) from the flashing of the lean absorbent, to generate a pressure in the reclaimer that is lower than the pressure in the regeneration column, and a reboiler (11) for carrying out the method, are described.

The present invention provides a process for removing ammonia as an aqueous salt solution from an acid gas comprising ammonia and hydrogen sulfide. A strong acid, such as sulfuric acid, is used as a scrubbing agent to convert ammonia to an ammonium salt. Control of pH and stripping in combination with reboiler or evaporators reduces hydrogen sulfide concentration. The ammonium salt is produced as an aqueous solution, which may crystallized to form a solid product. The ammonium salt solution or solid may be used as a fertilizer.

The invention discloses a solar aided carbon dioxide trapping integrated system, which mainly comprises three parts, i.e. a power generation subsystem, a carbon dioxide trapping subsystem and a solar heat collection subsystem, wherein the subsystems are connected mainly through a boiler feed water heater, a reboiler and a flue gas pretreatment device to form the whole integrated system. According to the system, the high and low energy requirements of related parts among the solar heat collection subsystem, the power generation subsystem and the carbon dioxide trapping subsystem are reasonably allocated and integrated in different connecting ways at the heat output end of the solar heat collection subsystem to realize the gradient utilization of energy, so that the energy consumption of extraction of vapor from a steam turbine of a power plant can be greatly reduced, the stability of the power plant can be maintained, the dual effects of utilizing renewable energy resources and reducing the carbon dioxide emission of the power plant are achieved, and the large-scale application of solar energy and an integrated flue gas trapping technology in China are forcefully promoted.

The invention provides a method for producing liquefied natural gas by using coke oven gas. The method comprises the following steps: (1) the coke oven gas is pretreated to remove benzene, naphthalene, tar and HCN (hydrogen cyanide); (2) sulfur is removed; (3) carbon is removed and the coke oven gas is dried; (4) the coke oven gas is led to a first heat exchanger and pre-cooled; (5) the pre-cooled coke oven gas passes through a second heat exchanger, a reboiler at the bottom of a low-temperature rectifying tower and a third heat exchanger in sequence, so that the temperature is lowered step by step; (6) gaseous liquid coming out of the third heat exchanger is led to a gas-liquid separator for gas-liquid separation, then the liquid coming out of the gas-liquid separator enters the low-temperature rectifying tower, and a liquefied natural gas product is acquired at the bottom of the low-temperature rectifying tower; and otherwise, the gaseous liquid coming out of the third heat exchanger is directly led to the low-temperature rectifying tower, and the liquefied natural gas product is acquired at the bottom of the low-temperature rectifying tower. The method for producing the liquefied natural gas by using the coke oven gas as raw material has the advantages of high output as well as low energy consumption and cost, and is easy to operate.

A process for low-temp separation of methane from coal seam gas and concentrating it includes such steps as removing O2, pressurizing, desulfurizing, decarbonizing, drying. Low-temp separation to obtain liquid methane, flowing in the condenser on the tower top for using it as the cold source of condensing reflux, and flowing the evaporated methane through heat exchanger to obtain product. Its purity is 95-99%. Its recovery rate is 95-99%.

The invention relates to a method for preparing high-purity cyclopentadiene, which comprises the following steps of: heating a thermal decomposer containing purified conduction oil and a composite inhibitor and a rectifying reboiler to a specified temperature; adding dicyclopentadiene serving as a crude product into the thermal decomposer continuously and stably; allowing the depolymerized cyclopentadiene to enter a rectifying column; extracting high-purity cyclopentadiene from a tower top, heating a small amount of dicyclopentadiene and by-products by the reboiler at the tower bottom to rectify the small amount of dicyclopentadiene and by-products again, and recycling kettle liquid. The method has the advantages of simple equipment, high production capacity, little coking and long service life of the conduction oil serving as a raw material and the equipment.

A refinery or petrochemical plant may include a fractionation column and related equipment, such as one or more condensers, receivers, reboilers, feed exchangers, and pumps. The equipment may have boundaries or thresholds of operating parameters based on existing limits and / or operating conditions. Illustrative existing limits may include mechanical pressures, temperature limits, hydraulic pressure limits, and operating lives of various components. There may also be relationships between operational parameters related to particular processes. For example, the boundaries on a naphtha reforming reactor inlet temperature may be dependent on a regenerator capacity and hydrogen-to-hydrocarbon ratio, which in turn may be dependent on a recycle compressor capacity. Operational parameters of a final product may be determined based on actual current or historical operation, and implemented in one or more models to determine adjustments for enhanced operational efficiency.

The invention relates to a method for treating wastewater containing phenol and ammonia, in particular to an energy-saving process for recycling the wastewater containing the phenol and the ammonia. Equipment among an acid removing tower, an ammonia removing tower and a water tower is coupled, namely a crude ammonia condenser on the top of the ammonia removing tower is taken as a reboiler of the acid removing tower and the water tower; and a differential pressure rectification technology is utilized, so that the step comprehensive utilization of a heat resource is realized, the energy consumption of wastewater treatment is reduced, and the using amount of steam and circulating water is greatly saved; particularly the equipment is coupled, the differential pressure rectification technologyis utilized and the ammonia and the phenol in the coal gasification wastewater are recycled simultaneously, so that the aims of saving energy and reducing emission in the wastewater treatment and recycling process are fulfilled. The technical problem that the energy consumption is high when the wastewater containing the phenol and the ammonia is recycled in the coal gasification process is solved; and the comprehensive utilization of energy is realized, and the method is high in social value and economic value.

The invention relates to a trichlorosilane three-tower differential pressure coupling energy-saving rectifying and purifying system and an operating method. The trichlorosilane three-tower differential pressure coupling energy-saving rectifying and purifying system comprises a primary tower, a secondary tower and a tertiary tower; the three towers are connected in series from low pressure to highpressure or from high pressure to low pressure, and a condensation re-boiler is arranged between the primary tower and the secondary tower and between the secondary tower and the tertiary tower respectively; and the three towers can be used for light removal, heavy removal and light removal in turn, and also can be used for combining light removal, heavy removal and light removal. According to the characteristics of approach full tower composition and approach temperature in the process of rectifying the trichlorosilane, the invention provides a trichlorosilane differential pressure coupling rectifying process which is expected to greatly reduce the production cost and energy consumption and theoretically rectify and save energy by nearly 70 percent. The technology remarkably improves themarket competitiveness of polycrystal silicon materials and promotes the development of a photovoltaic and information material industry chain.