A continuous phosphate crystallization system and a phosphate manufacturing method. The continuous phosphate crystallization system comprises a monoammonium phosphate production system (100), an integrated continuous crystallizer (7), a crystallization circulation pump (9), a crystallization heater (10), a crystallization vacuum condensation system (11), a crystallization material pump (12), a thickener (13), and a centrifuge (15), wherein a raw material input end of the integrated continuous crystallizer (7) is configured to be connected to a raw material phosphoric acid of a second concentration and an ammonia gas, or to be connected to a monoammonium phosphate slurry output end of the monoammonium phosphate production system (100), a circulating material output end of the integrated continuous crystallizer (7) is connected to a circulating material input end by means of the crystallization circulation pump (9) and the crystallization heater (10) in sequence, a crystallized material output end is connected to an input end of the centrifuge (15) by means of the crystallization material pump (12) and the thickener (13) in sequence, and the centrifuge (15) outputs a phosphate to be dried. The method comprises: delivering a raw material phosphoric acid of a first concentration in the range of 40-58% to the monoammonium phosphate production system (100) to obtain flash steam and a monoammonium phosphate slurry, and delivering the monoammonium phosphate slurry into the integrated continuous crystallizer (7) to obtain a crystallized material; or, delivering a raw material phosphoric acid of a second concentration in the range of 75-85% and an ammonia gas into the integrated continuous crystallizer (7) to obtain a crystallized material; and sequentially performing thickening, centrifugation and drying on the crystallized material to obtain a phosphate.
A low-energy consumption and low-emission fluidized bed urea granulation system, comprising: an ammonia recovery tower (P), a fluidized bed granulator (A), a first screening machine (B), a second screening machine (F), a cooler (C), a first bucket elevator (E), a second bucket elevator (D), a combined dust collector (J) and a melting tank (L).
B01J 2/16 - Processes or devices for granulating materials, in generalRendering particulate materials free flowing in general, e.g. making them hydrophobic by suspending the powder material in a gas, e.g. in fluidised beds or as a falling curtain
B01D 50/20 - Combinations of devices covered by groups and
3.
EMISSION REDUCTION DEVICE FOR AMMONIA IN GRANULATION EXHAUST GAS FROM UREA PRODUCTION DEVICE
An emission reduction device for ammonia in granulation exhaust gas from a urea production device. The emission reduction device comprises a combined tower body (1), a deamination section (2) arranged at a lower portion inside the combined tower body (1), and an ammonia recovery section (3) arranged at an upper portion inside the combined tower body; and further comprises a partition plate (7) and a gas riser (8) that are arranged between the deamination section (2) and the ammonia recovery section (3), wherein the deamination section (2) and the ammonia recovery section (3) are in gas phase communication but not in liquid phase communication. The emission reduction device can be flexibly mounted in a granulation tower or a granulation plant, has low investment costs and operation costs, and has a prolonged service life.
A vertical combined urea synthesis reactor (21) and a system comprising same and co-producing urea with offgas from a melamine plant. The vertical combined urea synthesis reactor (21) comprises: an upper reaction section (2), a lower stripping section (1), and a gas-liquid distributor (8) and a riser cap (12) that are arranged between the reaction section (2) and the stripping section (1). The system further comprises a melamine offgas condenser (22), a medium-pressure decomposition and recovery system (23), a low-pressure decomposition and recovery system (24) and a vacuum evaporation system (25), wherein offgas produced by the melamine plant, gas discharged through a gas outlet of the vertical combined urea synthesis reactor (21), and an ammonium carbamate solution from the medium-pressure decomposition and recovery system (23) are jointly fed into the melamine offgas condenser (22) to be condensed into a sub-high-pressure ammonium carbamate solution, and the sub-high-pressure ammonium carbamate solution in the melamine offgas condenser (22) is pressurized by a high-pressure ammonium carbamate pump (29), and is then fed into the combined urea synthesis reactor (21) through a high-pressure ammonium carbamate solution inlet for reaction.
C07C 273/04 - 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
C07C 273/12 - 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 combined with the synthesis of melamine
C07D 251/60 - Preparation of melamine from urea or from carbon dioxide and ammonia
B01J 19/24 - Stationary reactors without moving elements inside
An energy-saving urea production system, comprising a first synthesis tower (1), a second synthesis tower (6), a stripping tower (2), a high-pressure carbamate condenser (3), a high-pressure scrubber (4), a medium-pressure decomposition system (7), a low-pressure decomposition system (10), a vacuum pre-concentrator (9) and an evaporation concentration and granulation system (12). By means of the provision of the two synthesis towers, the urea synthesis conversion rate and the pressure of low-pressure steam produced as a by-product in the high-pressure carbamate condenser (3) are increased; and the medium-pressure decomposition system (7) diverges part of the load of the stripping tower (2), and the low-pressure steam produced as a by-product is used, thereby reducing the energy consumption of the urea production system.
C07C 273/04 - 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
22 gas inlet at the bottom thereof and is provided with a reaction solution outlet and a gas outlet at the upper part thereof; the heat-exchange tube bundle is of a U-shaped tube structure, and by means of the heat-exchange tube bundle, a heat transfer medium takes away heat generated by the hydrolysis of methylammonium; the internals comprise an efficient tray; and a downcomer is supported by means of the efficient tray. The present invention solves the problems of an existing methylammonium condenser having a small heat transfer coefficient, a large tube-end stress, a large arrangement space and a high difficulty in terms of manufacturing and transport. The high-pressure methylammonium condenser has a small heat exchange area and a small tube-end stress, is convenient to arrange, is easy to manufacture and scale up, and is convenient to transport.
B01D 5/00 - Condensation of vapoursRecovering volatile solvents by condensation
F28D 7/06 - Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits having a single U-bend
C07C 273/04 - 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
7.
COMBINED UREA SYNTHESIS REACTION APPARATUS AND SYSTEM COMPRISING SAME
Disclosed are a combined urea synthesis reaction apparatus and a system comprising same. The combined urea synthesis reaction apparatus comprises: a methylammonium synthesis reaction section, urea synthesis reaction sections and tail gas washing sections, wherein the methylammonium synthesis reaction section is horizontally arranged at the lower portion of the apparatus, a plurality of urea synthesis reaction sections are all uniformly and vertically connected to a shell-side pass of the methylammonium synthesis reaction section, and a tail gas washing section is provided at the top of each urea synthesis reaction section. The present invention solves the problems of high investment in urea high-pressure loop reaction, a large number of critical high-pressure devices, complex process control, and the necessity for vertical arrangement of the high-pressure devices in a high-pressure loop within a high framework, leading to high civil engineering investment. The combined urea synthesis reaction apparatus of the present invention has a simple structure, high heat exchange efficiency, low investment and manufacturing costs, and ease of arrangement, and is conducive to device manufacturing and the size increase of an apparatus.
B01J 19/24 - Stationary reactors without moving elements inside
C07C 273/04 - 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
B01J 10/00 - Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particlesApparatus specially adapted therefor
8.
NOVEL CLAUS SYSTEM FOR RECOVERING SULFUR FROM ACID GAS
222 in the gas entering the conversion subsystem to reach a preset value 2:1. The conversion subsystem is used for carrying out a low-temperature catalytic reaction on high-temperature process gas discharged from the sulfur-producing combustion furnace, so as to generate elemental sulfur. By means of the technical optimization of the Claus process itself, the present invention improves the sulfur recovery rate, and further matching with a reasonable tail gas treatment process will reduce the costs and production energy consumption of sulfur recovery devices to a certain extent, thus improving the yield of sulfur.
F23G 7/06 - Methods or apparatus, e.g. incinerators, specially adapted for combustion of specific waste or low grade fuels, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
C01B 17/04 - Preparation of sulfurPurification from gaseous sulfur compounds including gaseous sulfides
9.
SULFUR-TOLERANT SHIFT SYSTEM FOR PRODUCING HYDROGEN OR HYDROGEN-RICH GAS
Disclosed in the present utility model is a sulfur-tolerant shift system for producing hydrogen or a hydrogen-rich gas, comprising: a raw material main pipe, a raw material gas preheater, a shift reactor set, a medium-pressure steam superheater and a medium-pressure waste heat boiler. The shift reactor set comprises two or more shift reactors; the raw material main pipe is divided into two branch pipes; the first branch pipe is connected to a tube side of the raw material gas preheater and then is connected to the inlet of a first shift reactor, and the outlet of the first shift reactor is connected to a shell side of the raw material gas preheater; the second branch pipe is combined with a line at the outlet of a shell side of the raw material gas preheater and then connected to the inlet of a second shift reactor; the outlet of the second shift reactor is sequentially connected to a tube side of the medium-pressure steam superheater and a tube side of the medium-pressure waste heat boiler and then enters a subsequent shift reactor; a medium-pressure boiler water supply line is connected to the inlet of a shell side of the medium-pressure waste heat boiler; the outlet of the shell side of the medium-pressure waste heat boiler is divided into two paths, one path is connected to the inlet of the first shift reactor, and the other path enters a shell side of the medium-pressure steam superheater. According to the present utility model, the temperature of a catalyst bed of the first shift reactor is controlled by means of chemical balance, thereby thoroughly solving the over-temperature problem of catalyst beds, and prolonging the service life of catalysts. Only part of a raw material gas passes through the first shift reactor, and steam consumption of devices is reduced by adjusting loads of the first shift reactor and the second shift reactor.
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
C01B 3/12 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
10.
RADIANT TUBE SYSTEM STRUCTURE AND NATURAL GAS REFORMER COMPRISING SAME
A radiant tube system structure and a natural gas reformer comprising same. The radiant tube system structure comprises an inlet gas collection header (1), a gas delivery header (6), and a plurality of parallel radiant tube arrangements, wherein each parallel radiant tube arrangement includes an inlet distribution tube (2), outlet collection tubes and a plurality of parallel radiant tubes; each parallel radiant tube comprises an inlet pigtail tube (3), a reforming tube (4) and an outlet connection tube which are connected in sequence from top to bottom, and every two parallel radiant tubes are symmetrically distributed on two sides of an inlet distribution tube, the inlet pigtail tubes being horizontally connected perpendicular to the axis of the inlet distribution tube, and the outlet connection tube at an outlet of each parallel radiant tube being connected to an outlet collection tube, thereby forming one parallel radiant tube arrangement; and a plurality of parallel radiant tube arrangements are connected in parallel, a plurality of inlet distribution tubes at an inlet being connected to the inlet gas collection header, and outlet collection tubes at an outlet being connected to the gas delivery header, thereby forming a parallel radiant tube array. By means of symmetrical structures in which the inlet pigtail tubes are connected to two horizontal sides of each inlet distribution tube, and structural measures for reducing thermal differential stress, such as pre-biasing the installation of the top of each reforming tube, providing expansion holes in a base plate (10), and the outlet collection tubes, thermal stress in the entire tube system due to high-temperature expansion during operation can be effectively reduced.
A low-carbon emission ammonia synthesis system having an adjustable urea, ammonia and carbon imbalance, comprising: a natural gas two-stage conversion subsystem, a conversion gas purification subsystem, a fresh gas drying subsystem and an ammonia synthesis and refrigeration subsystem; natural gas raw material is passed through the natural gas two-stage conversion subsystem and the conversion gas purification subsystem, to generate fresh gas and carbon dioxide, and the fresh gas is sent to the fresh gas drying subsystem, to remove moisture by means of a molecular sieve; at the same time, on the basis of the output of carbon dioxide, a portion of the dried fresh gas is used as molecular sieve regeneration gas, and then sent back to the natural gas two-stage conversion subsystem as supplemental fuel gas, the remaining fresh gas is passed through the ammonia synthesis and refrigeration subsystem to produce a liquid ammonia product, and a balance of ammonia and carbon can be achieved in urea co-production. This solves the problem of a urea unit not being able to completely consume an ammonia product produced by an ammonia synthesis unit, reduces CO2 content in first stage furnace flue gas, achieves low carbon emissions, and can also reduce water content in the ammonia synthesis product and improve the purity of the ammonia synthesis product.
2222)) required by methanol synthesis of fresh gas can be flexibly adjusted in the present invention by arranging pre-conversion and a large steam reforming bypass or a small steam reforming bypass, hydrogen does not need to be additionally supplemented, that is, a hydrogen recovery unit does not need to be arranged, and the thermal load of a steam reforming furnace can be effectively reduced by arranging the bypass, thereby reducing the size of the steam reforming furnace.
Disclosed in the present utility model is a new fire tube type high-pressure waste heat boiler, comprising: a front-end tube box, a high-temperature section shell pass cylinder, a middle tube box, a low-temperature section shell pass cylinder and a rear-end tube box, which are connected in sequence; a high-temperature section heat exchange tube bundle arranged in the high-temperature section shell pass cylinder; a low-temperature section heat exchange tube bundle arranged in the low-temperature section shell pass cylinder; and a center tube, the inner center of which penetrates from the front-end tube box to the rear-end tube box and directly communicates the front-end tube box with the rear-end tube box, wherein the front-end tube box is sequentially in communication with the high-temperature section heat exchange tube bundle, the middle tube box, the low-temperature section heat exchange tube bundle and the rear-end tube box; flexible tube plates are provided at two ends of the high-temperature section shell pass cylinder and two ends of the low-temperature section shell pass cylinder; and a reinforcing rib is provided at a front portion in the high-temperature section shell pass cylinder, and the reinforcing rib is connected to the flexible tube plates. The fire tube type high-pressure waste heat boiler in the present utility model uses a two-section structure, and is also provided with the reinforcing rib and the flexible tube plates, such that the problem of strength failure of the tube plates and tube heads under high-temperature and high-pressure working conditions can be effectively solved, and the problem of excessive structural stress brought about by the up-scaling of devices and apparatuses can also be effectively solved.
F22B 1/18 - Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
14.
HIGH-PRESSURE UREA SOLUTION PRESSURE-REDUCING AND ENERGY-SAVING DEVICE FOR UREA DEVICE AND PROCESS METHOD
A high-pressure urea solution pressure-reducing and energy-saving device for a urea device, comprising a hydraulic turbine (1), a liquid level adjustment valve (2), a power device (3) driven by the hydraulic turbine (1), and a manual remote control adjustment valve (4). A third solution outlet (4.2) of the manual remote control adjustment valve (4) is connected to a first solution inlet (1.1) of the hydraulic turbine (1); one path of a high-pressure urea solution is connected to a second solution inlet (2.1) of the liquid level adjustment valve (2), and the other path is connected to a third solution inlet (4.1) of the manual remote control adjustment valve (4); and a first gas-liquid outlet (1.2) of the hydraulic turbine (1) and a second gas-liquid outlet (2.2) of the liquid level adjustment valve (2) are both linked to medium-pressure and low-pressure procedures. Further disclosed is a process method for a high-pressure urea solution pressure-reducing and energy-saving device for a urea device. A large amount of pressure energy lost on the liquid level adjustment valve in the pressure reduction process can be recycled by the hydraulic turbine driving the power device, such that the power consumption of the urea device is greatly reduced; and if the hydraulic turbine needs to be shut down for maintenance, all urea solutions are adjusted by means of the liquid level adjustment valve, and the maintenance is easy.
F01D 15/08 - Adaptations for driving, or combinations with, pumps
C07C 273/04 - 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
patents