WO2012011845A1 - Установка и способ для получения карбамида - Google Patents
Установка и способ для получения карбамида Download PDFInfo
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- WO2012011845A1 WO2012011845A1 PCT/RU2011/000527 RU2011000527W WO2012011845A1 WO 2012011845 A1 WO2012011845 A1 WO 2012011845A1 RU 2011000527 W RU2011000527 W RU 2011000527W WO 2012011845 A1 WO2012011845 A1 WO 2012011845A1
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- carbon dioxide
- liquid
- gaseous
- reactor
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
- C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
- C07C273/04—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
Definitions
- the invention relates to devices and methods for producing urea.
- a known installation for producing urea from ammonia and carbon dioxide at elevated temperature and pressure including a reactor, means for feeding liquid ammonia, liquid and gaseous carbon dioxide to the reactor, a device for evaporating liquid carbon dioxide by heat exchange through a wall with a coolant (Technical Gases, 2009 , N ° 2, p. 24).
- a known installation for producing urea from ammonia and carbon dioxide at elevated temperature and pressure containing a high pressure section, which includes a urea synthesis reactor containing means for feeding liquid ammonia, gaseous carbon dioxide and liquid carbon dioxide to the high pressure section
- a device for contacting a stream of liquid carbon dioxide with a stream of another reagent, namely, liquid ammonia comprising a housing with means for introducing liquid th carbon dioxide, liquid ammonia input and output the mixed stream, and also disposed within the housing coaxially with the housing convergent nozzle connected to the means for introducing liquid carbon dioxide.
- the known installation also contains a stripper, a condenser and a scrubber in the high-pressure section, means for supplying liquid flows from the reactor to the stripper, from the stripper at the stage of carbamide and recirculated liquid flow, from the condenser to the reactor, from the scrubber to the condenser, means for supplying gas flows from the reactor to the scrubber, from the stripper to the condenser, means for supplying a recirculated liquid stream to the scrubber (WO 2009/043365, C07C 273/04, 2009, p. 13, lines 1-8, 14-27, Fig. 5, 6) .
- a known method of producing urea at elevated temperature and pressure in a plant containing a high-pressure section which includes a reactor, stripper, condenser and scrubber, the method includes the interaction of ammonia and carbon dioxide in the reactor with the formation of the reaction mixture and separate conclusion from the reactor of a liquid stream containing urea, ammonium carbamate and free ammonia in an aqueous solution, and a gas stream containing mainly inert gases, the supply of liquid and gaseous to the high-pressure section carbon dioxide, supplying a liquid stream from the reactor to the stripper for partially decomposing ammonium carbamate and partially separating free ammonia in a stream of carbon dioxide gas introduced into the stripper to obtain a gas stream comprising ammonia and carbon dioxide mixed with water vapor, and a liquid stream including urea and residual ammonium carbamate in aqueous ammonia solution, supplying a liquid stream from the stripper at the stage of subsequent decomposition of ammonium carbamate and separation of ammonia and
- a known method for producing urea in a plant containing a high pressure section which includes at least a urea synthesis reactor at high pressures and temperatures, the method comprising supplying liquid and gaseous carbon dioxide streams to the high pressure section, and liquid carbon dioxide is introduced into the apparatus of the high-pressure section after mixing with another process stream, namely with liquid ammonia (WO 2009/043365, C07C 273/04, 2009, p. 13, lines 1-8, Fig. 5).
- the known method is implemented in an installation in which, in addition to the reactor, the high-pressure section also contains a stripper, condenser and scrubber.
- the method includes reacting ammonia and carbon dioxide in the reactor to form a reaction mixture and separately withdrawing from the reactor a liquid stream containing urea, ammonium carbamate and free ammonia in an aqueous solution, and a gas stream containing mainly inert gases, a gas stream from the reactor to the scrubber, a liquid stream from the reactor to the stripper for partially decomposition of ammonium carbamate and partial liberation of free ammonia in a stream of gaseous carbon dioxide introduced into the stripper to produce a gas stream including ammonia and carbon dioxide mixed with water vapor, and a liquid stream including urea and residual ammonium carbamate in aqueous ammonia solution, supplying a liquid stream from stripper at the stage of subsequent decomposition of ammonium carbamate and separation of ammonia and carbon dioxide to obtain urea and a recirculated liquid stream containing carbamide ammonia in an aqueous ammonia solution, supplying a gas stream from a stripper to
- a disadvantage of the known installation and the known method is the significant possibility of erosive damage to equipment.
- a rapid reaction of the formation of ammonium carbamate proceeds with the release of a large amount of heat, as a result of which the temperature in the mixing zone can increase even to higher values than the temperature in the reactor or condenser.
- the possibility of damage to the equipment due to the occurrence of cavitation phenomena only moves from one device to another.
- the problem solved by the invention is to improve the equipment and technology for the production of urea using liquid carbon dioxide.
- the technical result to which the invention is directed is to increase the reliability of the equipment used.
- a plant for producing urea from ammonia and carbon dioxide at elevated temperatures and pressures, containing a high-pressure section, which includes at least a carbamide synthesis reactor containing means for supplying liquid ammonia, gaseous carbon dioxide, and liquid carbon dioxide to a high-pressure section, a device for contacting a liquid carbon dioxide stream with a stream of another reagent, comprising a housing with means for introducing liquid carbon dioxide ode, another reactant input and output the mixed stream, and also disposed within the housing coaxially with the housing convergent nozzle connected to the means for introducing liquid carbon dioxide, characterized in that the device for housing contacting the liquid carbon dioxide stream with the stream of another reagent includes, as a means for introducing another reagent, means for introducing a gaseous reagent, as well as an insert of variable cross section inside the body coaxially to the body in the form of a pipe, the inlet portion of which is tapering, and the outlet is expanding, moreover, the insert is
- the high-pressure section of the proposed installation may consist of a urea synthesis reactor; in this case, the means for introducing the gaseous reactant into the device for contacting the liquid carbon dioxide stream with the gaseous reactant stream is means for introducing the carbon dioxide gas.
- the high-pressure section may also include a stripper, a condenser, and a scrubber operating at practically the same pressure as the reactor, means for supplying liquid flows from the reactor to the stripper, from the stripper at the stage of urea and recirculated liquid stream separation, from the condenser to the reactor, from a scrubber to a condenser, means for supplying gas flows from the reactor to the scrubber, from a stripper to a condenser, means for supplying a recirculated liquid stream to the scrubber.
- the means for introducing the gaseous reagent into the device for contacting the liquid carbon dioxide stream with the gaseous reagent stream may be either means for introducing the gaseous carbon dioxide or means for introducing the gaseous stream leaving the stripper or condenser.
- a method for producing urea from carbon dioxide and liquid ammonia in an installation containing a high-pressure section which includes at least a carbamide synthesis reactor at high pressures and temperatures, the method comprising supplying liquid and carbon dioxide gas, and the liquid carbon dioxide stream is introduced into the apparatus of the high-pressure section after mixing with another process stream, characterized in that the liquid dioxide stream and carbon is contacted with a gaseous reactant stream in a device for contacting a liquid carbon dioxide stream with a gaseous reactant stream used in the proposed installation, when a liquid stream is fed into an insert of variable cross-section through a tapering nozzle, and a gaseous stream into a housing, liquid carbon dioxide is vaporized by contacting it in the insert with a part of the gaseous reactant stream entering the insert, followed by contacting the mixed stream after exiting inserts with the rest of the gaseous reactant stream passing through the annular gap between the insert and the housing.
- a carbon dioxide gas stream is used as a gaseous reactant stream to be contacted with a liquid carbon dioxide stream, and the mixed stream is sent to the reactor.
- the high-pressure section contains a stripper, condenser and scrubber, it is preferable to separate from the reactor a liquid stream containing urea, ammonium carbamate and free ammonia in an aqueous solution, and a gas stream containing mainly inert gases, a feed gas flow from the reactor to the scrubber, supplying a liquid stream from the reactor to the stripper for partial decomposition of ammonium carbamate and partial separation of free ammonia in a stream of gaseous diode introduced into the stripper carbon monoxide to obtain a gas stream comprising ammonia and carbon dioxide mixed with water vapor, and a liquid stream including urea and residual ammonium carbamate in an aqueous ammonia solution, supplying a liquid stream from
- both a gaseous carbon dioxide stream and a gaseous stream leaving the stripper or condenser can be used to contact the liquid carbon dioxide stream. If as a stream of gaseous reagent directed to contact with the stream liquid carbon dioxide, use a stream of gaseous carbon dioxide, the stream obtained by mixing these streams is sent to the stripper. If a stream leaving a stripper is used as a stream of a gaseous reagent directed to contact with a liquid carbon dioxide stream, the stream obtained by mixing these streams is sent to a condenser. If a stream leaving a condenser is used as a stream of a gaseous reagent directed to contact with a liquid carbon dioxide stream, then the stream obtained by mixing these streams is sent to the reactor.
- the mass ratio between liquid carbon dioxide and that part of the gaseous stream that is contacted with the liquid carbon dioxide stream inside the insert according to the proposed method should be such that the liquid carbon dioxide completely evaporates in the interior of the insert without significant overheating.
- this ratio can vary over a fairly wide range, for example, from 1: 0.5 to 1: 2.5.
- the amount of heat transferred from the gaseous reactant stream to the liquid carbon dioxide stream may, at low temperatures of liquid carbon dioxide, be insufficient for the complete conversion of liquid carbon dioxide into gas. This can cause droplets of the liquid phase to enter the inner wall of the pipeline and cause cavitation-erosion disturbances.
- Means for transferring liquid and gas flows from one apparatus of the high-pressure section to another can be made in the form of pipelines that provide gravity flow.
- ejectors can be used as such means, for example, for injecting a liquid stream from a scrubber with a liquid ammonia stream, injecting a gas stream from a stripper with a liquid ammonia stream and / or an ammonium carbamate solution stream, and the like.
- a device for contacting the flows of liquid and gaseous carbon dioxide is mounted on the pipeline as its section.
- the use of the insert in the design of the device allows you to protect the walls of the high pressure pipeline from cavitation-erosion damage and increase the reliability of the equipment used.
- FIG. 1-6 The invention is illustrated by the attached FIG. 1-6.
- FIG. 1-6 In FIG.
- FIG. 1 shows a schematic flow diagram of the proposed installation implementing the proposed method, in which the high-pressure section contains a reactor
- FIG. 2 is a design of an apparatus for contacting liquid carbon dioxide and gaseous reactant streams.
- FIG. Figures 3-6 are schematic flow diagrams of variants of the proposed installation, in which, in addition to the reactor, the high-pressure section contains a stripper, a condenser and a scrubber.
- a plant for producing urea from carbon dioxide and liquid ammonia at high pressures and temperatures includes a urea synthesis reactor 1, a pump 2 for feeding liquid ammonia to a reactor 1, a compressor 3 for supplying gaseous carbon dioxide to a reactor 1, and a pump 4 for feeding liquid carbon dioxide into reactor 1, device 5 for contacting the streams of liquid carbon dioxide and gaseous reagent.
- the device 5 consists of a cylindrical body 6, a nozzle 7 for introducing a gaseous reactant, a nozzle 8 for introducing a liquid carbon dioxide, a nozzle 9 for discharging a mixed gaseous stream.
- the nozzle 8 is connected to a nozzle 10 located coaxially to the housing 6 and tapering towards the outlet fitting 9.
- a nozzle 10 located coaxially to the housing 6 and tapering towards the outlet fitting 9.
- An annular gap 12 is formed between the insert 11 and the inner surface of the housing 6, which also has a variable cross section.
- the insert 11 is fixed inside the housing 6 using the support plates 13.
- the cut of the nozzle 10 can be located in the same plane with the inlet of the insert 11, or inside the insert 11.
- Installation for producing urea from carbon dioxide and liquid ammonia which implements the proposed method, works as follows.
- Liquid ammonia is fed to pump 2 by a pump 2.
- Gaseous carbon dioxide from compressor 3 and liquid carbon dioxide from pump 4 are fed to a device 5 for contacting carbon dioxide flows.
- Gaseous carbon dioxide enters the device 5 through the nozzle 7.
- a stream of liquid carbon dioxide enters the device and is directed to the tapering nozzle 10.
- the stream of liquid carbon dioxide is accelerated and at the exit of the nozzle forms a conical flare from droplets of liquid dispersed in gaseous medium.
- the torch opens inside insert 1 1.
- a moving stream of liquid droplets entrains gas coming from nozzle 7 into insert 11.
- the desired ratio between the liquid carbon dioxide stream and the carbon dioxide gas stream entering the interior of the insert is ensured by an appropriate choice of design parameters of the device 5 determined by calculation based on known methods.
- the droplet stream starts to work like a piston and transport gas from the inlet section of the insert 11 to its outlet section into the free space inside the device 6 in the direction of the nozzle 9.
- urea melt is formed, which is a water-ammonia solution of urea and ammonium carbamate not converted to urea, which is separated by known evaporation and condensation processes, injecting the finished urea in crystalline or granular form.
- Dispersion of the liquid plume in the gas phase in the device 5 allows you to create a significant surface area of the liquid-gas contact, and the difference in gas and liquid velocities contributes to turbulence and mixing of the liquid and gas flows. All this contributes to the efficient flow of heat and mass transfer in the flare. Due to the transfer of heat from hot gas to liquid, it is heated and evaporated. At the outlet of insert 11, liquid carbon dioxide is completely converted to gas. After the cooled gas stream exits from the insert 11 into the free space inside the housing 6, this cold gas stream is mixed with the rest of the hot carbon dioxide gas passing through the gap 12 between the inner surface of the housing 6 and the insert 11. As a result of the contacting of these two flows, the temperature rises cold mixed gas flow due to the heat of the rest of the gaseous carbon dioxide.
- the insert 11 not only allows you to create the optimal geometry of the flow part for the effective contacting of the flows of liquid carbon dioxide with gaseous, but also protects the walls of the housing 6 from contact with drops of liquid carbon dioxide. It is known that when a gas-liquid mixture moves in a pipeline, especially during a phase transition, cavitation-erosion damage is observed on the inner surface of the pipeline. Especially dangerous are such phenomena at high pressure. Box 11 is not designed for high pressure, as located inside the housing 6, and the thickness of its wall is much smaller than the wall thickness of the housing, designed for high pressure. Therefore, the metal content of the insert is small, and it can be made of a material resistant to cavitation-erosion phenomena, and can also be replaced if it is worn.
- the gap 12 between the insert 11 and the inner surface of the housing 6 has a variable cross-sectional area along the length of the insert 11.
- the narrowing of the insert 11 at its initial section provides flow injection efficiency carbon dioxide gas.
- the expansion of the insert 11 and the narrowing of the slit 12 at the outlet of the insert 11 allows to increase the flow rate of gaseous carbon dioxide at the exit of the slit 12, which contributes to a more efficient mixing of the flows of cold and hot gas in the free volume of the device after insert 11.
- the support plates 13, fixing the insert inside the housing 6, can be made at an angle to the flow of moving gas.
- the 3 high-pressure section of the urea plant includes a reactor 1, pumps 2 and 4 for supplying liquid ammonia and liquid carbon dioxide, a compressor 3 for supplying gaseous carbon dioxide, a device 5 for mixing flows of liquid and gaseous carbon dioxide, a stripper 14, a condenser 15, and a scrubber 16 operating at almost the same pressure, an ejector 17, a pipe 18 for supplying a stream of carbon dioxide from a pump 4 to a device 5, a pipe 19 for supplying a stream of carbon dioxide from a compressor 3 to a device 5, a wire 20 for supplying a stream of carbon dioxide from the device 5 to the stripper 14, a pipe 21 for supplying liquid ammonia to the ejector 17, a pipe 22 for supplying a liquid stream from the reactor 1 to the stripper 14, a pipe 23 for supplying a liquid stream from the stripper 14 in the urea separation step and recirculated liquid stream (not shown in FIG.
- the apparatus shown in FIG. 3, works as follows. Liquid carbon dioxide from pump 4 through line 18 and gaseous carbon dioxide from compressor 3 through line 19 enters a device 5 for mixing these streams, which functions in the same way as described above with respect to FIG. 2.
- the mixed gas stream from the device 5 enters through pipeline 20 to the lower part of stripper 14, where most of the ammonium carbamate is decomposed in a stream of carbon dioxide and when steam is heated, and part of the excess ammonia is distilled off from the urea melt (aqueous ammonia solution of urea and ammonium carbamate) formed in the reactor 1.
- Liquid flow from the lower part the stripper 14 through the pipe 23 serves at the stage of the final decomposition of ammonium carbamate and ammonia distillation with the release of urea and the formation of a recycled liquid stream containing ammonium carbamate in a water-ammonia solution, which is passed through a pipe 28 to a scrubber 16.
- a gaseous mixture of carbon dioxide, ammonia and water vapor from the upper part of the stripper 14 is passed through a pipe 27 to a condenser 15, where the gas condensation-absorption process occurs as a result of their mixing with ammonia and aqueous ammonium carbamate solution while cooling with boiling steam condensate.
- a mixture of ammonia and an aqueous solution of ammonium carbamate enters the condenser 15 through a pipe 31 from an ejector 17, where ammonia is supplied from a pump 2 through a pipe 21, and an aqueous solution of ammonium carbamate from a scrubber 16 through a pipe 29.
- a quantity of urea melt from the bottom of the reactor 1 may also enter the ejector 17.
- the concentrated aqueous ammonia solution of ammonium carbamate and non-condensed gases from the condenser 15 enter through pipelines 24 and
- FIG. 4 differs from the embodiment depicted in FIG. 3, in that the device 5 is designed to mix the liquid carbon dioxide stream supplied by the pump 4 through the pipe 18 and the gaseous stream coming from the stripper 14 through the pipe 27 with a mixed gaseous stream supplied to the condenser 15 through the pipe 20.
- a variant of the process flow diagram of the proposed installation, depicted in FIG. 5 differs from the embodiment depicted in FIG. 4, only by the fact that the pipelines 20 and 31 are connected not with the upper, but with the lower part of the capacitor 15, the pipeline 24 is connected not with the lower, but with the upper part of the capacitor 15 and is intended for joint supply of liquid and gas flows from the condenser 15 to the reactor 1 and the pipeline 25 is missing.
- a variant of the process flow diagram of the proposed installation depicted in FIG. 6 differs from the embodiment depicted in FIG. 3, in that the device 5 is intended for mixing the liquid carbon dioxide stream supplied by the pump 4 through the pipe 18 and the gaseous stream coming from the condenser 15 through the pipe 25 with a mixed gaseous stream into the reactor 1 through the pipe 20, and also by the fact it further comprises an ejector 32 for injecting a gas stream from the stripper 14 coming through the pipe 27, the stream coming from the ejector 17 through the pipe 33, and the output of the ejector 17 is connected by a pipe 31 to the bottom of the capacitor 15.
- EXAMPLE 1 In accordance with FIG. 1 and 2, carbamide synthesis reactor 1, operating at a pressure of 20 MPa and a temperature of 185 ° C, is supplied with 13,200 kg / h of liquid ammonia by a pump 2, 2500 kg / h of liquid carbon dioxide with a temperature of from -25 to + 15 ° C by pump 4 and 12500 kg / h of carbon dioxide gas with a temperature of 130 ° C by compressor 3. The flows of liquid and gaseous carbon dioxide are mixed in the contacting device 5.
- EXAMPLE 2 The process is carried out analogously to example 1 with the difference that 4300 kg / h of liquid carbon dioxide with a temperature of from -25 to + 15 ° C supplied by pump 4 and 10700 kg / h of carbon dioxide gas are mixed in contacting device 5 temperature of 130 ° C supplied by compressor 3.
- 70 to 90% of the carbon dioxide gas stream is entrained (the mass ratio of the liquid and gaseous carbon dioxide flows in the inner space of the insert is from 1: 1.74 to 1: 2.24 ), which provides full pr rotation of the liquid carbon dioxide in the gas inside the insert 11.
- the mixed flow with a temperature of 73-88 ° C is then contacted in the housing 6 with the rest of the device (10-30%) hot stream of gaseous carbon dioxide.
- the flow of gaseous carbon dioxide has a temperature of 80-95 ° C.
- EXAMPLE 3 The process is carried out analogously to example 1 with the difference that in the device for contacting 5 mixed 5000 kg / h of liquid carbon dioxide with a temperature of from -25 to + 15 ° C supplied by pump 4, and 10000 kg / h of gaseous carbon dioxide with temperature of 130 ° C supplied by compressor 3.
- the mass ratio of the liquid and gaseous carbon dioxide flows in the inner space of the insert is 1: 1, 8 to 1: 1, 96 ), which provides full revraschenie liquid carbon dioxide in the gas inside the insert 11.
- EXAMPLE 5 The process is carried out analogously to example 4 with the difference that 14339 kg / h of liquid carbon dioxide with a temperature of from -25 to + 15 ° C supplied by pump 4 and 32979 kg / h of gaseous carbon dioxide are mixed with contacting device 5 a temperature of 90-100 ° C supplied by the compressor 3 (the ratio of the flows of carbon dioxide is 1: 2.3). 70-75% of the carbon dioxide gas stream is entrained into the inner space of insert 11 (FIG. 2), which ensures the complete conversion of liquid carbon dioxide into gas inside insert 11. A mixed stream with a temperature of 50-58 ° C is then contacted in housing 6 (FIG. 2) devices with the rest of (25-30%) of a hot stream of gaseous carbon dioxide. At the exit of the device 5, the flow of gaseous carbon dioxide has a temperature of 57-65 ° C.
- EXAMPLE 6 The process is carried out on the installation, a diagram of which is shown in FIG. 4. 20,000 kg / h of liquid carbon dioxide with a temperature of -25 to + 15 ° C from pump 4 through line 18 through the nozzle 8 (Fig. 2) and 110,000 kg / h of a gaseous stream (a mixture of carbon dioxide, ammonia and water vapor from the upper part of the stripper 14) with a temperature of 180-190 ° C through the pipe 27 through the nozzle 7 (Fig. 2) enter the device 5 for mixing these flows. A moving stream of liquid droplets carries with it into the insert 11 (Fig.
- the liquid stream from the bottom of the stripper 14 (120000 kg / h) through a pipe 23 serves at the stage of the final decomposition of ammonium carbamate and ammonia distillation with the release of 62500 kg / h of urea and the formation of 40500 kg / h of a recirculated liquid stream containing ammonium carbamate in aqueous ammonia solution, which ory via line 28 enters a scrubber 16 Mixed gas stream from nozzle 9 (Fig.
- a mixture of ammonia and an aqueous solution of ammonium carbamate enters the condenser 15 through a pipe 31 from an ejector 17, where ammonia is supplied from a pump 2 through a pipe 21, and an aqueous solution of ammonium carbamate from a scrubber 16 through a pipe 29.
- ammonia is supplied from a pump 2 through a pipe 21
- an aqueous solution of ammonium carbamate from a scrubber 16 through a pipe 29.
- phase separation occurs in the upper part of the reactor 1, phase separation occurs.
- the liquid phase (urea melt) flows through line 22 to stripper 14, and the gas phase, which consists mainly of inert gases with an admixture of ammonia, passes through line 26 to scrubber 16, where ammonia is further absorbed by contact with the recirculated liquid stream entering the scrubber 16 through the pipeline 28. Gases from the scrubber 16 are sent through the pipeline 30 to the stage of formation of the recirculated liquid stream for their final purification from ammonia.
- EXAMPLE 7 The process is carried out analogously to example 6 on the installation, a diagram of which is shown in FIG. 5, with the corresponding difference that the flows from the device 5 and the ejector 17 do not flow through the pipelines 20 and 31 to the lower but the lower part of the condenser 15, and the gas-liquid mixture formed in the condenser 15 is discharged from the upper part of the condenser 15 through a pipeline 24 to the reactor 1.
- EXAMPLE 8 The process is carried out analogously to example 6 on the installation, a diagram of which is shown in FIG. 6.
- 20,000 kg / h of liquid carbon dioxide with a temperature of -25 to -15 ° C from pump 4 through a pipe 18 and 12000 kg / h of gaseous flow (a mixture of carbon dioxide, ammonia and water vapor from the top of the condenser 15) with a temperature of 170 -175 ° C through pipeline 25 enter the device 5 for mixing these flows.
- the device 5 operates in the same way as in the installation, the circuit of which is shown in FIG. 5.
- a moving stream of liquid droplets entrains 90-95% of the gaseous stream inside the insert And (Fig.
- Liquid ammonia 35500 kg / h
- aqueous solution of ammonium carbamate 50500 kg / h
- a certain amount of urea melt from the bottom of the reactor 1 can also enter.
- the liquid stream from the bottom of the stripper 14 (120,000 kg / h) is fed through line 23 to the stage of final decomposition of ammonium carbamate and ammonia distillation with the release of urea and the formation of a recirculated liquid stream containing ammonium carbamate in an aqueous ammonia solution, which through line 28 enters the scrubber 16.
- the gas stream from stripper 14 (110000 kg / h) through line 27 arrives into the ejector 32, the working stream of which is the liquid stream coming from the ejector 17 through the pipe 33.
- the mixed gas-liquid stream from the ejector 32 enters through the pipe 31 to the condenser 15, where at a pressure of 13.5-14.5 MPa and a temperature of 165-175 ° C, the process of condensation-absorption of gases occurs as a result of their mixing with ammonia and an aqueous solution of ammonium carbamate when cooled by boiling steam condensate.
- the reactor 1 and the scrubber 16 operate in the same way as in the installation, the diagram of which is shown in FIG. 5.
- the invention can be used in the chemical industry and the fertilizer industry.
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UAA201215114A UA102666C2 (ru) | 2010-07-20 | 2011-07-18 | Установка и способ для производства карбамида |
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RU2010130523 | 2010-07-20 | ||
RU2010130523/04A RU2434850C1 (ru) | 2010-07-20 | 2010-07-20 | Установка и способ для получения карбамида |
RU2010141629/04A RU2440977C1 (ru) | 2010-10-11 | 2010-10-11 | Способ и установка для получения карбамида |
RU2010141629 | 2010-10-11 |
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Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US11806683B2 (en) | 2020-06-09 | 2023-11-07 | Metso Outotec Finland Oy | Fluidizing nozzle and fluidized bed reactor |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
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US2087325A (en) * | 1933-09-13 | 1937-07-20 | Solvay Process Co | Process for the production of urea and ammonium salts |
RU2309947C1 (ru) * | 2006-06-05 | 2007-11-10 | Открытое Акционерное Общество "Научно-Исследовательский И Проектный Институт Карбамида И Продуктов Органического Синтеза" (Оао Ниик) | Способ и установка для получения карбамида и способ модернизации установки для получения карбамида |
WO2009043365A1 (en) * | 2007-10-04 | 2009-04-09 | Urea Casale S.A. | Process and plant for urea production |
EA200900790A1 (ru) * | 2006-12-08 | 2009-12-30 | ДСМ АйПи АССЕТС Б.В. | Способ получения мочевины |
-
2011
- 2011-07-18 WO PCT/RU2011/000527 patent/WO2012011845A1/ru active Application Filing
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2087325A (en) * | 1933-09-13 | 1937-07-20 | Solvay Process Co | Process for the production of urea and ammonium salts |
RU2309947C1 (ru) * | 2006-06-05 | 2007-11-10 | Открытое Акционерное Общество "Научно-Исследовательский И Проектный Институт Карбамида И Продуктов Органического Синтеза" (Оао Ниик) | Способ и установка для получения карбамида и способ модернизации установки для получения карбамида |
EA200900790A1 (ru) * | 2006-12-08 | 2009-12-30 | ДСМ АйПи АССЕТС Б.В. | Способ получения мочевины |
WO2009043365A1 (en) * | 2007-10-04 | 2009-04-09 | Urea Casale S.A. | Process and plant for urea production |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US11806683B2 (en) | 2020-06-09 | 2023-11-07 | Metso Outotec Finland Oy | Fluidizing nozzle and fluidized bed reactor |
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