CN1100412A - Stripping recirculation technology & apparatus for urea production - Google Patents
Stripping recirculation technology & apparatus for urea production Download PDFInfo
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- CN1100412A CN1100412A CN 93117513 CN93117513A CN1100412A CN 1100412 A CN1100412 A CN 1100412A CN 93117513 CN93117513 CN 93117513 CN 93117513 A CN93117513 A CN 93117513A CN 1100412 A CN1100412 A CN 1100412A
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Abstract
The present invention aims at solving the problems of available techn, and the said techn includes adopting binary anticorrosive in the equipment, introducing oxygen-rich tail gas at the bottom of medium-pressure decomposer to inactivate medium-pressure equipment and condensing the medium pressure decomposed gas mainly in heat-recovering section at the bottom of evaporator. With less high-pressure equipment and reasonable structure, the said techn can produce urea in short period, and with low energy consumption and low cost.
Description
The invention belongs to the urea production field.
As everyone knows, industrial with the existing in the world so far multiple production method of ammonia and carbon dioxide production urea, can be divided into two big classes usually: i.e. water solution total cycling method and vaporizing extract process.Water solution total cycling method is early stage process for producing urea, and its representative flow process has the water solution total cycling method of Si Tamibang company; Recycle to extinction C method, the D method of Mitsui/eastern pressure company; The total recycle processes of Montecatini etc., this is high energy consumption one class methods.The vaporizing extract process urea production is the technology of the sixties and later development thereof, and its representative flow process has the CO of Si Tamibang company
2Vaporizing extract process is (hereinafter to be referred as CO
2Vaporizing extract process); The ammonia vaporizing extract process of SNAM S.P.A.; The isobaric double flow formulation (IDR method) of Montedisons SPA; The saving energy and cost novel process of Mitsui/eastern pressure company (being called for short the ACES method).They are to use CO
2, NH
3Or two kinds of process for producing urea that all use as steam stripping agent, have characteristic of low energy consumption.
CO at above-mentioned Si Tamikabang
2In the vaporizing extract process technology, the equipment in the high pressure circle synthesis includes: synthetic tower, and stripping tower, high pressure condenser, high pressure scrubber, they are all operated under same pressure, remove this and also have two steam pocketss.The synthetic tower working pressure is 13.7MPa(g), service temperature 183-185 ℃, NH
3/ CO
2(mol)=and 2.8-2.9, H
2O/CO
2(mol)=0.34, Synthesis conversion is 57%, and stripping tower goes out 167 ℃ of liquid temps, contains NH in the solution
37.8%, contain CO
210%; Pay producing steam pressure 0.32-0.34MPa(g).
CO
2The stripping genealogy of law adopts low ammonia carbon ratio, low working pressure, and the technological operation that comes the reinforced high pressure circle promptly reaches the concentration stripping of stripping tower, the concentration absorption of high pressure scrubber, presses circulation section in cancelling with this, and the solution behind the stripping directly arrives low-pressure stage.The drawback of bringing like this is that equipment corrosion is big, and needing increases the passivation air capacity, causes tail gas to enter limits of explosion, and equipment need make explosion-proof type, increases and takes off H
2System etc.The short advantage of flow process has not just existed like this, and reduction of equipment effective rate of utilization and energy consumption are high relatively.Because the restriction of operational condition, the operating restraint of this method is very narrow, elasticity is little, and operational stability is poor, and device is difficult to realize long-term operation.Age afterwards is with CO for this reason
2The technology that gas the is made steam stripping agent several new technological process (comprising stripping circulation method of the present invention) that grown up again.
In the saving energy and cost novel process (ACES method) of above-mentioned Mitsui/eastern pressure company, the equipment in the high pressure circle synthesis has: urea synthesizer, CO
2Stripping tower, first and second high pressure methylamine condenser, high pressure scrubber, they are all operated under same pressure, also have two steam pocketss in addition.The working pressure of urea synthesizer is: pressure 17.1MPa (g), 190 ℃ of temperature, NH
3/ CO
2(mol)=4.0, H
2O/CO
2(mol)=0.64, Synthesis conversion 68% is paid producing steam pressure 0.5MPa(g).This technology system adopts high ammonia carbonization, and high working pressure is to improve conversion rate of urea.But its high-tension apparatus platform number is many, and operation link is many, and operation easier is big, the individual device complex structure, and manufacture difficulty is big, and total cost of equipment increases.The protection against corrosion air capacity that this technology adds is big, and oxygen level is raw material CO
20.5% of gas, this has not only reduced the effective rate of utilization of equipment, and the hydrogen-oxygen ratio has reached limits of explosion in the intermediate pressure section tail gas, and the device operation is very dangerous.
The purpose of new stripping circulation method urea production process of the present invention and device thereof is intended to design a kind of energy-saving urea production process and device thereof with new characteristic, it is low that this technology has energy consumption, and flow process is brief, and turndown ratio is big, the operational safety good reliability, advantages such as low equipment investment.
New stripping circulation method urea production process of the present invention includes high pressure circle synthesis, middle pressure circulation section and low-pressure recirculation section, and it is with CO
2Stripping circulation method urea production process as steam stripping agent is characterized in that:
(1). the high pressure circle synthesis has only four high-tension apparatuses, i.e. synthetic tower 4, stripping tower 5, hp ammonium carbamate condenser 6, high pressure scrubber 7, these four equipment are in same stress level, utilize potential difference to carry out the material circulation each other, wherein:
(a). synthetic tower 4 adopts common multi-deck screen template, and its operating parameters is: pressure 15.5-16.5MPa(g), and temperature 185-190 ℃, NH
3/ CO
2(molecular ratio) 3.5-3.7, H
2O/CO
2(molecular ratio) 0.6-0.7, urea synthesis transformation efficiency 65-67%;
(b). the tower inside of stripping tower 5 is divided into upper and lower two portions, and top is the filler branch device and the tubulation liquid distributor of solution, promptly sets up a packing layer above former tubulation liquid divides size, rises to distribute and refinery distillation, to save steam, improves steam stripping efficiency; The bottom is the falling film type tube still heater, and its operating parameters is: pressure 15.5-16.5MPa (g), go out 170-175 ℃ of tower solution temperature, and go out tower solution ammonia content 11-13%;
(c). high pressure methylamine condenser 6 adopts still formula U-shaped tube heat-exchanger, the Guan Chengwei processing medium, shell is the generation low-pressure steam, interchanger and steam inclusion and one, its operating parameters is: pressure 15.5-16.5MPa (g), and temperature 170-175 ℃, shell is byproduct steam pressure 0.4-0.6MPa (g), this structure operation is easy, can also reduce by an independent steam pockets;
(d). high pressure scrubber 7 adopts sieve-plate structures, in establish three tower trays, only play adiabatic sorption;
(2). in high pressure loop, adopt the anticorrosion passivator of binary, promptly remove at CO
2Gas adds outside the air before advancing compressor 1, and flows into the ingress adding hydrogen peroxide (H of stripping tower 5 at the reactant of synthetic tower 4
2O
2), satisfying the needs, particularly service temperature height of the anticorrosion and safety operation of system device, extent of corrosion is wanted the anticorrosion needs of big stripping tower relatively.The add-on of binary sanitas is: air 0.20-0.25%(is with O
2Meter), hydrogen peroxide (H
2O
2) be 1.5-2.5Kg/T(urea); Hydrogen peroxide preferably adds system with the form of aqueous hydrogen peroxide solution;
(3). at middle pressure circulation section, M.P.decomposer 8 adopts and has the separator of packing layer and the structure that the falling film type tube still heater is combined, top is rectifying section and tubulation liquid distributor, the bottom is falling film type tube still heater (this heater tube be and be divided into two sections), and the first ammonium in the solution is heated at this and is decomposed into CO
2, NH
3Required heat, epimere is supplied with by low-pressure steam, and hypomere is supplied with by the middle pressure steam phlegma that stripping tower comes, the oxygen enrichment tail gas of introducing high pressure scrubber 7 in the bottom of M.P.decomposer 8 plays the stripping effect simultaneously with passivation medium voltage network equipment in the falling film type tubulation of M.P.decomposer; The operating parameters of M.P.decomposer 8 is: amount of pressure 1.6-1.8MPa (g), decomposition temperature 155-160 ℃;
(4). at middle pressure circulation section, it is the energy recovery section that is one section vacuum-evaporator 22 lower case that the condensation of middle pressure decomposition gas absorbs, first ammonium separator 11, in press that resorber 12 and coupled pipeline form in push back in the receipts system and carry out, pressing decomposition gas to be used for being concentrated into the urine of vacuum-evaporation operation in the heat of condensation of one section vacuum-evaporator 22 energy recovery section, heat of condensation at middle pressure resorber 12 is removed with the temperature adjustment water coolant, is tower tray at middle pressure resorber 12 by horizontal condenser and epimere, hypomere is that the absorption tower of filler is formed, the absorption tower two sections are adiabatic sorption section, the ammonium bicarbonate solution that comes with dual circulation process condensate and low-pressure stage is made absorption agent respectively, and the temperature of middle pressure condenser system first ammonium liquid is 100-110 ℃;
(5). in low-pressure recirculation section, low pressure splitter 9 tops are packing section, the bottom is a falling film type tubulation heating zone, be recovered in the low pressure recovery system that low-pressure condenser 14, ammonium fluid storage tank 15, ammonium fluid pump 16, low pressure absorption tower 17, low pressure absorbent recirculation pump 18, low pressure absorb recirculation cooler 19 and the pipeline that is connected is formed from the gas of low pressure splitter 9 and desorption tower 32, the working pressure of this system is 0.1-0.3MPa(g).
The flow process of new stripping circulation method urea production process of the present invention is seen Fig. 1: CO
2The compressed machine 1 of gas is gone into the bottom of stripping tower 5, for protection against corrosion, at the inlet CO of compressor
2Add 0.20-0.25%(in the gas with O
2Meter) air.Liquid NH
3Through high-pressure ammonia pump 2, liquefied ammonia preheater 3 is gone into the bottom of synthetic tower 4, and reaction mixture is separated into gas phase and liquid phase at cat head.Liquid phase mixture is gone into stripping tower 5 tops, adds hydrogen peroxide (H at this
2O
2) the aqueous solution, to strengthen the anticorrosion of stripping tower, in stripping tower, solution is gone into the falling film type tube still heater through filler distribution device and tubulation liquid distributor, shell is uses 2.2MPa(g) the saturation steam heating, first ammonium in the solution and superfluous ammonia are at heating and counter current contact CO
2Be decomposed under the stripping effect of gas and separate, the gas that goes out the stripping tower top is gone into hp ammonium carbamate condenser 6, mix with the first ammonium liquid of high pressure scrubber 7 and partial condensation at this gas, heat of condensation is used for pay producing a 0.4-0.6MPa(g) steam, the gas-liquid mixture that goes out carbamate condenser is gone into the bottom of synthetic tower 4.In synthetic tower, material is through certain residence time, CO wherein
2And NH
3Continue reaction production first ammonium, reaction heat is used to improve the interior temperature of charge of tower and provides the first ammonium to change into the heat of urea.The gas phase that goes out the synthetic tower top is gone into high pressure scrubber 7, at this portion C O
2And NH
3The first ammonium amine liquid of being sent here by first ammonium pump 13 carries out the thermal insulation absorption, and the liquid after the absorption is gone into hp ammonium carbamate condenser 6, and the tail gas that discharge at the top is gone into the bottom of M.P.decomposer 8.
The solution that goes out stripping tower 5 is gone into the space on M.P.decomposer 8 tops through decompression, passed through the top packing layer of distribution and refinery distillation then, go into the falling film type tube still heater of bottom again through the uniformly distributing of tubulation distribution head, the first ammonium in the solution is heated at this and is decomposed into CO
2, NH
3, needed heat is supplied with by low-pressure steam at the well heater epimere, steams phlegma at hypomere by the middle pressure of stripping tower 5 and supplies with.Introduce oxygen enrichment tail gas from high pressure scrubber 7 in the bottom of M.P.decomposer 8 with passivation medium voltage network equipment, in the falling film type tubulation of splitter, play the stripping effect simultaneously.
The working pressure of M.P.decomposer 8 is 1.6-1.8MPa(g), decomposition temperature is 155-160 ℃.
The solution that goes out M.P.decomposer 8 bottoms is gone into low pressure splitter 9 through regulator of level, and the structure of low pressure splitter 9 also is the structure that falling film type tube still heater and splitter group lump together with M.P.decomposer 8.In low pressure splitter 9, first ammonium remaining in the solution further resolves into CO
2, NH
3, decompose required heat and supply with by low-pressure steam.The working pressure of low pressure splitter 9 is 0.15-0.30MPa (g), and decomposition temperature is 135-140 ℃.
The urine that goes out low pressure splitter 9 is gone into flash drum 10 through regulator of level, and its working pressure is 0.044MPa, and urine is gone into one section vacuum-evaporator 22 or urine groove 20 then.
The gas that goes out M.P.decomposer 8 tops is gone into the hypomere of one section vacuum-evaporator 22, part CO in this gas with the first ammonium liquid of middle pressure resorber 12
2, NH
3Condensation, heat of condensation is used for concentrating urea solution, goes out the gas-liquid mixture that one section vacuum-evaporator, 22 hypomere shells are and goes into first ammonium separator 11, and first ammonium liquid is gone into high pressure scrubber 7 through high pressure carbamate pump 13, press resorber 12 to continue condensation during gas is gone into, heat of condensation is removed by temperature adjustment water.In horizontal, press condenser top to be provided with the absorption tower, this tower top is the column plate section, and the bottom is a packing section, and the column plate section is an absorption agent with the phlegma of dual circulation condensate pump 36, packing section absorbs with the solution spraying of ammonium fluid pump 16, and non-condensable gases enters atmosphere through pressure regulator valve.
Go out gas condensation in low-pressure condenser 14 of the gas and the desorption tower 32 of low pressure splitter 9, heat of condensation is removed with water coolant, gas-liquid mixture is gone into ammonium fluid storage tank 15 after the condensation, solution is pressed the packing section on resorber 12 absorption towers in ammonium fluid pump 16 parts are sent, part is as the phegma of desorption tower 32.Gas presses the phlegma of next solution of resorber 12 column plate sections and dual circulation condensate pump 36 to absorb to low pressure absorption tower 17 in the quilt.The noncondensable gas that goes out low pressure absorption tower 17 enters atmosphere through pressure regulator valve.
The technological process that the urine simmer down to is traditional.Urine from flash drum 10 is concentrated into 99.7% through 22, two sections vacuum-evaporators 23 of one section vacuum-evaporator, through melt urea pump 24, and prilling spry 25, prilling tower 26 obtains the granular urea product.One section evaporation operation pressure is the 0.027-0.033MPa(absolute pressure), service temperature is 128-130 ℃, the dual circulation working pressure is the 0.0033MPa(absolute pressure), service temperature is 138-140 ℃.From flash drum, one section vacuum-evaporator and two sections gas condensations in vacuum generating system 28 that vacuum-evaporator comes, vacuum generating system 28 is made up of surface condenser and steam injector, and heat of condensation is removed by water coolant, and lime set is gone into process condensate storage tank 29.
Process condensate from storage tank 29 contains small amount of N H
3, CO
2And urea, through desorption tower feeding pump 30, desorption tower preheater 31 is introduced desorption tower 32.Desorption tower 32 is formed by upper and lower two sections, and solution is by epimere column plate, NH wherein
3, CO
2Come out by stripping, the solution after the desorb is through hydrolyzer feeding pump 33, and hydrolyzer preheater 34 is gone into hydrolyzer 35, the urea in this solution under high temperature action and certain residence time be hydrolyzed into NH
3And CO
2, needed heat is provided by middle pressure steam.The solution that goes out hydrolyzer 35 is gone into the top of desorption tower 32 hypomere column plates after heat exchange, solution stream wherein NH when each column plate
3, CO
2Come out by the steam stripped that the bottom adds.The liquid of deriving from desorption tower 32 bottoms is almost pure water, and ammonia and urea content are discharged the battery limit (BL) and utilized less than 5ppm after heat exchange.The gas that desorption tower 32 tops and hydrolyzer 35 are derived is gone into low-pressure condenser 14.The working pressure of hydrolyzer 35 is 2.3MPa(g), the working pressure of desorption tower 32 is 0.3MPa(g).
A kind of urea technique will really can be realized industrialization, must reliable advanced person except technical process, rational device structure type selecting and good equipment and materials also to be arranged as assurance.Generate in the technology at new stripping circulation method urea of the present invention, it is basic identical with M.P.decomposer 8 that the specific equipment that is adopted mainly contains stripping tower 5, hp ammonium carbamate condenser 6, M.P.decomposer 8, low pressure splitter 9().All the other equipment and known CO
2The equipment that technology adopted such as vaporizing extract process, ACES method are similar basically.
In technology of the present invention, the stripping tower 5 that is adopted is energy-saving CO
2Stripping tower is promptly set up a packing layer simple for production above the former tubulation liquid distribution head of general stripping tower, promptly the filler distribution device has two portions up and down in the tower, and top is the filler distribution device and the tubulation liquid distributor of solution, and the bottom is the falling film type tube still heater.
The stripping tower of this kind structure, the packing layer on top can play the uniform distribution and the refinery distillation of material, and its setting can be played saving steam, improve the effect of steam stripping efficiency.See Fig. 2.
In technology of the present invention, hp ammonium carbamate condenser 6 adopts still formula U-shaped tube heat-exchanger, and Guan Chengwei processing medium, shell are the generation low-pressure steam, interchanger and steam inclusion and one.
This structure not only makes technological operation simple, can reduce by an independent steam pockets simultaneously, saves equipment manufacturing cost.See Fig. 3.
In technology of the present invention, M.P.decomposer 8 adopts and has the separator of packing layer and the structure that the falling film type tube still heater is combined, top is rectifying section and tubulation liquid distributor, the bottom is a falling film type tubulation heating zone, this heating zone pipe is and is divided into upper and lower two sections, last heating zone is used the low-pressure steam heating, and following heating zone is made thermal source by the steam condensate of stripping tower 5.
The structure of the structure of low pressure splitter 9 and M.P.decomposer 8 is basic identical, and its difference only is falling film type tube still heater part, and low pressure heater 9 only is one section.
In this unitized construction, the low pressure splitter, have the function of pre-separation and pre-rectifying, the residence time is short, the thermo-efficiency height is paid reaction and is well controlled.See Fig. 4.
Technology of the present invention is to optimize to transform on the basis of existing stripping circulation method urea production process and device thereof, the armamentarium manufacturing of can basing on our country, and compared with prior art, technology of the present invention has following advantage:
1. the ammonia carbon ratio that technology high-voltage circle of the present invention adopts is moderate, and processing condition relax, and the intermediate pressure section that is increased has been cancelled superfluous ammonia recovery system, compared with the CO of Si Tamikabang
2The vaporizing extract process turndown ratio is big, good stability, and processing ease is grasped, the unit service factor height;
2. the anticorrosion passivator of process using binary of the present invention, antiseptic property is good, has eradicated the combustion explosion source, device good operation safety, operation factor height;
3. middle pressure decomposition tower adopts falling film type tube still heater and the splitter group that has packing layer to lump together, function with pre-separation and pre-rectifying, and introduce the oxygen enrichment tail gas of high pressure section in its underpart, equipment that not only can the passivation medium voltage network makes NH contained in the gas
3, CO
2All reclaimed at intermediate pressure section, and played the stripping effect, thereby saved steam consumption.
4. the energy-saving CO of process using of the present invention
2Stripping tower is promptly set up a packing section simple for production on the top of general stripping tower, reaches gas, liquid is well distributed, promotes refinery distillation, greatly reduces the load of tubulation heating zone, thereby has saved steam;
5. the hp ammonium carbamate condenser of technology of the present invention adopts still formula U-shaped tube heat-exchanger, and shell is the generation low-pressure steam, and steam pockets and interchanger are one, independent steam pockets need not be established again,, liquid distributor etc. need not be established in the bobbin carriage compared with vertical tubulation carbamate condenser, designs simplification, the thermo-efficiency height;
6. handle the high pressure scrubber of synthetic tower gas phase, " ACES " method is a packing tower, CO
2Vaporizing extract process is an immersion tubular heat exchange and with the bigger explosion-proof space of a volume, complex structure, and operation inconvenience, cost is higher.Technology of the present invention is established the sieve-tray tower of three tower trays in being, only plays adiabatic sorption, need not what control, and easy to operate and safe;
7. for the high pressure circle synthesis, " ACES " method is five high-tension apparatuses, and is with two low-pressure steam bags, CO
2Vaporizing extract process is four high-tension apparatuses, is with two low-pressure steam bags, and new stripping circulation method urea production process of the present invention only is four high-tension apparatuses.On energy consumption, the steam consumption of technology of the present invention is close with " ACES " method, compares CO
2Vaporizing extract process is hanged down about 250Kg/ ton (urea).From investment, technology of the present invention and the CO that has increased dehydrogenation system
2Vaporizing extract process is approaching, than " ACES " method low about 10%.
8. the armamentarium of technology of the present invention can be based on domestic manufacturing, thereby can save a large amount of foreign exchanges for country, and reduces investment outlay.
Description of drawings:
Fig. 1: new stripping circulation method urea production process schema
Wherein:
1. press 23. 2 sections cold boilers of absorber 13. high pressure carbamate pump 14. low-pressure condensers, 15. ammonium fluid storage tank 16. ammonium fluid pumps, 17. low pressure absorption tower 18. low pressure absorbent recirculation pumps, 19. low pressure absorption cycle cooler 22. 1 sections cold boilers of 20. urine grooves, 21. urine pumps, 24. melt urea pumps, 25. prilling spries, 26. granulation towers, 27. belt conveyers, 28. vacuum generating systems, 29. process condensate storage tanks, 30. desorber feed pumps, 31. desorber preheaters, 32. desorbers, 33. hydrolyzer feed pumps, 34. hydrolyzer preheaters, 35. hydrolyzers in the compressor 2. high-pressure ammonia pumps 3. liquefied ammonia preheaters 4. synthetic towers 5. strippers 6. hp ammonium carbamate condensers 7. high pressure scrubbers 8. M.P.decomposers 9. low pressure decomposers 10. flash tanks 11. first ammonium separators 12.
MS middle pressure steam CW water coolant PIC pressure-regulator (indication control)
LS low-pressure steam TW temperature adjustment water coolant PRC pressure-regulator (meter record control)
SC steam condensate HC remote control LIC regulator of level (indication control)
Fig. 2: stripping tower structural representation
Wherein:
1. the synthetic liquid of tubulation liquid distributor 2. fillers 3. 4. pneumatic outlet 5.CO that enter the mouth
2Gas 6. urea solns that enter the mouth export 7. steam-ins, 8. condensate outlets 9,10. manhole
Fig. 3: hp ammonium carbamate condenser structural representation
Wherein:
1. restrain 2. bobbin carriages, 3. gas inletes 4. gas liquid outlets, 5. vapour outlets, 6. relief valve connections, 7. vapor condensations inlet 8. steam-in 9. manholes that go into operation
Fig. 4: M.P.decomposer structural representation
Wherein:
1. filler 2. tubulation liquid distributors 3. tubulations 4. pump liquid 5. pneumatic outlets, 6. oxygen enrichment gas inlets, 7. urines that enter the mouth export 8. low-pressure steam and enter the mouth to press in 9. condensate outlets 10. and press cold liquid outlet in the cold liquid inlet 11.
Claims (4)
1, a kind of include high pressure circle synthesis, middle pressure circulation section and low-pressure recirculation section with CO
2Stripping circulation method urea production process as steam stripping agent is characterized in that:
(1). the high pressure circle synthesis has only four high-tension apparatuses, i.e. synthetic tower (4), stripping tower (5), hp ammonium carbamate condenser (6), high pressure scrubber (7), these four equipment are in same stress level, utilize potential difference to carry out the material circulation each other, wherein:
(a) synthetic tower (4) adopts common multilayer sieve plate tower, and its operating parameters is: pressure 15.5-16.5MPa (g), temperature 185-190 ℃, NH
3/ CO
2(molecular ratio) 3.5-3.7, H
2O/CO
2(molecular ratio) 0.6-0.7, urea synthesis transformation efficiency 65-67%;
(b) the tower inside of stripping tower (5) is divided into upper and lower two portions: top is filler distribution device and tubulation liquid distributor, the bottom is the falling film type tube still heater, its operating parameters is: pressure 15.5-16.5MPa (g), go out 170-175 ℃ of tower solution temperature, and go out tower solution ammonia content 11-13%;
(c) hp ammonium carbamate condenser (6) adopts still formula U-shaped tube heat-exchanger, the Guan Chengwei processing medium, shell is the generation low-pressure steam, interchanger and steam inclusion and one, its operating parameters is: pressure 15.5-16.5MPa (g), temperature 170-175 ℃, shell is byproduct steam, and its pressure is 0.4-0.6MPa (g);
(d) high pressure scrubber (7) adopts sieve-plate structure, in establish three tower trays, only play adiabatic sorption;
(2). in high pressure loop, adopt the anticorrosion passivator of binary, promptly remove at CO
2Gas advances compressor (1) and adds outside the air before, and flows into the ingress adding hydrogen peroxide (H of stripping tower (5) at the reactant of synthetic tower (4)
2O
2), to satisfy the needs of the anticorrosion and safety operation of system device, the add-on of binary sanitas is: air 0.20-0.25% (in 02), hydrogen peroxide (H
2O
2) be 1.5-2.5Kg (H
2O
2)/T (urea), hydrogen peroxide preferably adds system in the mode of the aqueous solution;
(3). at middle pressure circulation section, M.P.decomposer (8) adopts and has the separator of packing layer and the structure that the falling film type tube still heater is combined, top is rectifying section and tubulation liquid distributor, the bottom is falling film type tube still heater (this heater case is and is divided into upper and lower two periods), and the first ammonium in the solution is heated at this and is decomposed into CO
2, NH
3Required heat, epimere is supplied with by low-pressure steam, hypomere is supplied with by the middle pressure steam phlegma that stripping tower comes, introduce the next oxygen enrichment tail gas of high pressure scrubber (7) with passivation medium voltage network equipment in the bottom of M.P.decomposer (8), simultaneously play the stripping effect in the falling film type tubulation of M.P.decomposer, the operating parameters of M.P.decomposer (8) is: pressure 1.6-1.8MPa (g), decomposition temperature 155-160 ℃;
(4). at middle pressure circulation section, the condensation absorption of middle pressure decomposition gas is the energy recovery section in one section vacuum-evaporator (22) bottom, first ammonium separator (11), push back in the receipts system in the middle pipeline composition of pressing resorber (12) and being connected and carry out, the middle decomposition gas of pressing is in the condensation of one section vacuum-evaporator (22) energy recovery section, its heat of condensation is used for being concentrated into the urine of vacuum-evaporation operation, heat of condensation at middle pressure resorber (12) is removed with the temperature adjustment water coolant, it is tower tray by horizontal condenser and epimere that middle pressure is inhaled haustorium (12), hypomere is that the absorption tower of filler is formed, on the absorption tower, following two sections is adiabatic sorption, the ammonium bicarbonate solution that comes with dual circulation process condensate and low-pressure stage is made absorption agent respectively, and the condensing temperature of middle pressure condenser system first ammonium liquid is 100-110 ℃;
(5). in low-pressure recirculation section, low pressure splitter (9) top is packing section and tubulation liquid distributor, the bottom is a falling film type tubulation heating zone, be recovered in the low pressure recovery system that low-pressure condenser (14), ammonium fluid storage tank (15), ammonium fluid pump (16), low pressure absorption tower (17), low pressure absorbent recirculation pump (18), low pressure absorb recirculation cooler (19) and the pipeline that is connected is formed from gas that low pressure splitter (9) and desorption tower (32) come, the working pressure of this system is 0.1-0.3MPa (g).
2, by the specific equipment of the described technology of claim 1, it is characterized in that described stripping tower (5) is an energy-saving CO
2Stripping tower is promptly set up a filler distribution device simple for production on the top of general stripping tower, and upper and lower two portions are arranged in the tower, and top is the filler distribution device and the tubulation liquid distributor of solution, and the bottom is the falling film type tube still heater.
By the specific equipment of the described technology of claim 1, it is characterized in that 3, described hp ammonium carbamate condenser (6) adopts still formula U-shaped tube heat-exchanger, Guan Chengwei processing medium, shell are the generation low-pressure steam, interchanger and steam inclusion and one.
4, press the specific equipment of the described technology of claim 1, it is characterized in that, described M.P.decomposer (8) adopts and has the separator of packing layer and the structure that the falling film type tube still heater is combined, its top is the rectifying separation section of filler and tubulation liquid distributor, the bottom is a falling film type tubulation heating zone, this lower heating section is divided into upper and lower two sections again: go up heating zone and use the low-pressure steam heating, following heating zone uses the middle pressure steam phlegma that is come by stripping tower to make thermal source.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN93117513A CN1039413C (en) | 1993-09-16 | 1993-09-16 | Stripping recirculation technology & apparatus for urea production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN93117513A CN1039413C (en) | 1993-09-16 | 1993-09-16 | Stripping recirculation technology & apparatus for urea production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1100412A true CN1100412A (en) | 1995-03-22 |
| CN1039413C CN1039413C (en) | 1998-08-05 |
Family
ID=4992050
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN93117513A Expired - Fee Related CN1039413C (en) | 1993-09-16 | 1993-09-16 | Stripping recirculation technology & apparatus for urea production |
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| Country | Link |
|---|---|
| CN (1) | CN1039413C (en) |
Cited By (12)
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| CN101397144B (en) * | 2007-10-22 | 2010-05-26 | 贵州赤天化股份有限公司 | Method for absorbing ammonia by cooling down of high pressure shift temperature water from stripping urea plant |
| CN101628883B (en) * | 2009-08-10 | 2012-05-30 | 四川金象赛瑞化工股份有限公司 | Urea mid pressure decomposing process adopting double heating-falling film countercurrent heat exchange |
| CN102635536A (en) * | 2012-05-03 | 2012-08-15 | 内蒙古乌拉山化肥有限责任公司 | Method for preventing CO2 from being liquefied in five-section type CO2 compressor |
| CN103408467A (en) * | 2013-08-08 | 2013-11-27 | 中国五环工程有限公司 | Low-energy-consumption urea production technology and system adopting CO2 stripping method |
| CN103724232A (en) * | 2013-12-24 | 2014-04-16 | 天津市昊永化工科技有限公司 | Energy-saving optimization technology of deep hydrolysis system for improving urea production capacity |
| CN103781761A (en) * | 2011-09-09 | 2014-05-07 | 乌里阿·卡萨勒有限公司 | A carbon dioxide stripping urea plant with a natural-circulation synthesis loop and a method for retrofitting such plant |
| CN104284883A (en) * | 2012-05-03 | 2015-01-14 | 斯塔米卡邦有限公司 | Urea production plant |
| CN104387296A (en) * | 2014-10-28 | 2015-03-04 | 河南骏化发展股份有限公司 | Production technique of urea |
| CN104402768A (en) * | 2014-11-03 | 2015-03-11 | 河南晋开化工投资控股集团有限责任公司 | Technology for producing urea from low-purity liquefied ammonia as raw material |
| CN109516932A (en) * | 2018-12-19 | 2019-03-26 | 安徽节源环保科技有限公司 | A kind of process system of equipment Reform for Energy Saving of Urea Plant |
| CN110041230A (en) * | 2019-04-30 | 2019-07-23 | 中国五环工程有限公司 | Recycle the vaporizing extract process urea production process of melamine plant tail gas |
| CN113233415A (en) * | 2021-05-24 | 2021-08-10 | 大连理工大学 | Process and device for preparing hydrogen from hydrogen iodide in iodine-sulfur cycle |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63112552A (en) * | 1986-10-30 | 1988-05-17 | Toyo Eng Corp | Separation method for unconverted substance |
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1993
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101397144B (en) * | 2007-10-22 | 2010-05-26 | 贵州赤天化股份有限公司 | Method for absorbing ammonia by cooling down of high pressure shift temperature water from stripping urea plant |
| CN101628883B (en) * | 2009-08-10 | 2012-05-30 | 四川金象赛瑞化工股份有限公司 | Urea mid pressure decomposing process adopting double heating-falling film countercurrent heat exchange |
| CN103781761A (en) * | 2011-09-09 | 2014-05-07 | 乌里阿·卡萨勒有限公司 | A carbon dioxide stripping urea plant with a natural-circulation synthesis loop and a method for retrofitting such plant |
| CN103781761B (en) * | 2011-09-09 | 2016-08-24 | 卡萨莱股份有限公司 | A kind of carbon dioxide stripping urea plant using nature-circulation synthesis loop and the method reequiping this device |
| US9732033B2 (en) | 2012-05-03 | 2017-08-15 | Stamicarbon B.V. | Urea production plant |
| CN110003056A (en) * | 2012-05-03 | 2019-07-12 | 斯塔米卡邦有限公司 | Urea Preparation equipment |
| CN104284883A (en) * | 2012-05-03 | 2015-01-14 | 斯塔米卡邦有限公司 | Urea production plant |
| CN102635536A (en) * | 2012-05-03 | 2012-08-15 | 内蒙古乌拉山化肥有限责任公司 | Method for preventing CO2 from being liquefied in five-section type CO2 compressor |
| US9458098B2 (en) | 2012-05-03 | 2016-10-04 | Stamicarbon B.V. | Urea production plant |
| CN103408467B (en) * | 2013-08-08 | 2015-02-18 | 中国五环工程有限公司 | Low-energy-consumption urea production technology and system adopting CO2 stripping method |
| CN103408467A (en) * | 2013-08-08 | 2013-11-27 | 中国五环工程有限公司 | Low-energy-consumption urea production technology and system adopting CO2 stripping method |
| CN103724232B (en) * | 2013-12-24 | 2015-05-13 | 天津市昊永化工科技有限公司 | Energy-saving optimization technology of deep hydrolysis system for improving urea production capacity |
| CN103724232A (en) * | 2013-12-24 | 2014-04-16 | 天津市昊永化工科技有限公司 | Energy-saving optimization technology of deep hydrolysis system for improving urea production capacity |
| CN104387296B (en) * | 2014-10-28 | 2016-09-28 | 河南骏化发展股份有限公司 | A kind of urea production process |
| CN104387296A (en) * | 2014-10-28 | 2015-03-04 | 河南骏化发展股份有限公司 | Production technique of urea |
| CN104402768B (en) * | 2014-11-03 | 2016-10-05 | 河南晋开化工投资控股集团有限责任公司 | A kind of low-purity liquefied ammonia is the technique of raw material production carbamide |
| CN104402768A (en) * | 2014-11-03 | 2015-03-11 | 河南晋开化工投资控股集团有限责任公司 | Technology for producing urea from low-purity liquefied ammonia as raw material |
| CN109516932A (en) * | 2018-12-19 | 2019-03-26 | 安徽节源环保科技有限公司 | A kind of process system of equipment Reform for Energy Saving of Urea Plant |
| CN109516932B (en) * | 2018-12-19 | 2024-04-12 | 安徽节源环保科技有限公司 | Energy-saving reforming process system of urea device |
| CN110041230A (en) * | 2019-04-30 | 2019-07-23 | 中国五环工程有限公司 | Recycle the vaporizing extract process urea production process of melamine plant tail gas |
| CN110041230B (en) * | 2019-04-30 | 2021-10-15 | 中国五环工程有限公司 | Process for producing urea by stripping method for recovering tail gas of melamine device |
| CN113233415A (en) * | 2021-05-24 | 2021-08-10 | 大连理工大学 | Process and device for preparing hydrogen from hydrogen iodide in iodine-sulfur cycle |
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