CN1463964A - Water solution all-circulation aquadrate high pressure system energy-saving and production-increasing process - Google Patents
Water solution all-circulation aquadrate high pressure system energy-saving and production-increasing process Download PDFInfo
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Abstract
The present invention provides new technological process of producing urea in a completely circulating high pressure solution system. On the basis of available high pressure system, three pieces of high pressure apparatus including one urea synthesizing tower, one synthesizing tower separator and one gas stripping column are increased, the original urea synthesizing tower is altered into the second one, the first urea synthesizing tower is for feeding CO2 and ammonia only and the second urea synthesizing tower is for pressure lowering operation. The system of the present invention has one 30-100 % raised production capacity and greatly lowered power consumption.
Description
Technical field
The present invention relates to a kind of process for producing urea, specifically, is that the high-pressure system of aqueous solution complete circling urea device is carried out the novel process that energy-saving and production-increase is transformed.
Background technology
The middle-size and small-size urea plant of at present domestic total about 200 covers wherein mostly is the aqueous solution recycle to extinction Technology of Si Tamikabang company the fifties in last century, and in today of 21st century, this Technology is backward greatly.This technology exists and consumes height, tail gas easily fires contains problems such as ammonia and the pollution of urea severe overweight with effluent discharge, is badly in need of carrying out the transformation of energy-saving and production-increase.
The aqueous solution complete circling urea production technique of Si Tamikabang company, synthesis pressure 20MPa, 188 ℃ of synthesis temperatures, synthetic charging NH
3/ CO
2Than be 3.8～4.0, H
2O/CO
2Than being 0.65～0.7, synthetic tower CO
2Per pass conversion is 62～64%.This technology high-pressure system only has a urea synthesizer, and there is a big difference with present advanced in the world urea technique technology.Anticorrosion oxygen-adding amount is big in this method two carbonoxide in addition, and tail gas easily fires, and domestic a lot of blast accidents takes place once.
For overcoming the problems referred to above that prior art exists, middle-size and small-size aqueous solution complete circling urea device to domestic a large amount of backwardnesss carries out the energy-saving and production-increase transformation, and granted patent ZL 97112476.0 (applying date is on June 13rd, 1997) provides a kind of aqueous solution complete circling urea device high pressure loop loop process that includes hp ammonium carbamate condenser, first urea synthesizer, high-pressure decomposition tower and second urea synthesizer.Through industrial pilot, because hp ammonium carbamate condenser is horizontal type structure, exists carbon dioxide and liquefied ammonia and be difficult to uniformly distributing and go into every U-shaped pipe, first ammonium pre-reaction zone can not be set easily cause in the heat transfer tube problems such as first crystalline ammonium obstruction to improve reaction mass as early as possible and enter the temperature of heat transfer tube and shell-side steam condensate preheating difficulty.The inventor is after the experience of summing up industrial pilot device operation, and it is simpler further to have developed flow process, and has overcome the another kind of water solution all-circulation aquadrate high pressure system energy-saving and production-increasing transformation novel process of many weak points of above-mentioned horizontal carbamate condenser.
Summary of the invention
The invention provides the novel process that a kind of aqueous solution complete circling urea device high-pressure system energy-saving and production-increase is transformed, it is the high-pressure system at the existing middle-size and small-size urea plant of aqueous solution recycle to extinction, increase small number of devices, and equipment is all in ground configuration, install simple, can put under the situation about not stopping production at the crude urine white, quiet clothes and transform, only the join dependency pipeline gets final product during annual overhaul.Adopting novel process of the present invention can make the crude urine white, quiet clothes put throughput increases by 30～100%, consume significantly to descend, and the expense of transforming only is equivalent to 30～40% of new device.
The aqueous solution complete circling urea device high-pressure system new energy-saving and production-increase process (see figure 1) that includes first urea synthesizer 1, synthetic tower separator 2, stripping tower 3 and second urea synthesizer 4 (utilizing original urea synthesizer) of the present invention, it is characterized in that, in existing aqueous solution complete circling urea device high-pressure system
(1) increase by one first urea synthesizer 1, this equipment is divided into first ammonium pre-reaction zone 10, first ammonium reaction zone 11 and urea and generates district's 12 3 parts.Only at bottom charging feed liquefied ammonia and carbonic acid gas, working pressure 20～21MpaG, 188～190 ℃ of service temperatures, charging NH
3/ CO
2Molecular ratio 3.6～3.8, CO
2Per pass conversion can reach more than 75%.The discharging of synthetic tower 1, the gas-liquid mixture that promptly contains urea, first ammonium, water, superfluous ammonia and small amounts of inert gas is sent into synthetic tower separator 2.
(2) increase a synthetic tower separator 2, the discharging at first urea synthesizer, 1 top is carried out gas-liquid separation at synthetic tower separator 2, then, the isolated liquid that contains urea, first ammonium, water, superfluous ammonia in bottom is decompressed to the top that 14.5～15.5MpaG delivers to stripping tower 3, isolated gas promptly contains little ammonia, carbonic acid gas and rich oxygen containing rare gas element and is decompressed to 14.5～15.5MpaG, deliver to the bottom of stripping tower 3, as passivation rot-resistant oxygen source.
(3) increase a stripping tower 3, the fluid of synthetic tower separator 2 is decompressed to 14.5～15.5MPaG through Liquid level adjusting valve, enter the top of stripping tower 3, behind packing layer, enter the falling film type well heater, adopt liquid dispenser on every tubulation top, make the liquid uniformly distributing and be membranaceous from top to bottom and flow along the tubulation inwall, shell-side is with the steam heating of 2.2～2.4MPaG, under high pressure decomposition and separation goes out first ammonium and the superfluous ammonia that major part does not get transformed into urea, thereby presses the load of decomposing system in reducing greatly.Stripping tower 3 fluids are decompressed to 1.7～1.8MpaG and deliver to the former middle decomposing system of pressing, and stripping tower 3 is given vent to anger and contained ammonia, carbonic acid gas, water and rich oxygen containing rare gas element, enters the bottom of second urea synthesizer 4.
(4) change former urea synthetic tower reduced pressure operation into second urea synthesizer 4, the first ammonium liquid of former M.P. absorber boosts to 14.5～15.5MPaG through former one section first ammonium pump, and giving vent to anger with stripping tower 3 enters the bottom of second urea synthesizer 4 in the lump.The working pressure of synthetic tower 4 is reduced to 14.5～15.4MPaG by former 20MPaG, 185～188 ℃ of service temperatures, charging NH
3/ CO
2Molecular ratio is 4.2～4.5, H
2O/CO
2Molecular ratio is 1.4～1.5, CO
2Transformation efficiency can reach 58～60%.The service temperature of synthetic tower 4 feeds a small amount of CO by the rate of decomposition of adjusting stripping tower 3 with in its bottom
2Realize.The fluid of second urea synthesizer 4 is decompressed to 1.7～1.8MPaG and stripping tower 3 fluids enter the former middle decomposing system of pressing in the lump, the rich oxygen containing part gas phase in second urea synthesizer, 4 tops is decompressed to 1.8MPaG by restriction orifice and delivers to former middle bottom of pressing decomposition heater as the anticorrosion required oxygen of this heating installation passivation, thereby can stop using the former air compressor machine that adds air to this equipment that is specifically designed to.
The lining and the tubulation of first urea synthesizer of the present invention (1), synthetic tower separator (2) and (3) three high-tension apparatuses of stripping tower all preferably adopt OOCr
25Ni
22Mo
2Material.
Technology of the present invention, wherein said first urea synthesizer 1 is divided into first ammonium pre-reaction zone 10, first ammonium reaction zone 11 and urea and generates district's 12 3 parts, reaction of first ammonium and urea generate all to be finished in first urea synthesizer 1, and fresh raw materials ammonia and carbonic acid gas are sent into from the bottom by the mouth of pipe 13 and 14 respectively.The tower bottom is a first ammonium pre-reaction zone 10, is provided with eddy flow plate 15 and gas distributor 16 in first ammonium pre-reaction zone 10, to accelerate mass transfer and rate of heat transfer, makes reactant reach temperature of reaction as early as possible, and the first ammonium liquid that reaction is generated forms internal recycle in this zone; The gas-liquid uniformly distributing goes into to be provided with the first ammonium reaction zone 11 continuation reactions of heat transfer tubulation 17 then, feed steam condensate between tubulation, utilize first ammonium reaction heat by-product 0.8～0.9MPaG low-pressure steam, and the reacting weight by steam regulation pressure-controlling first ammonium, thereby control tower top urea generate the district temperature, keep the thermal equilibrium of first urea synthesizer 1; In urea generates district 12, multi-layer efficient column plate 18 is set, can increase the gas-to-liquid contact interface, with well distributed gas phase, the phenomenon of back-mixing takes place in the interior liquid in increase gas-to-liquid contact interface and absolute anti-zone here owing to the severe difference, thereby can improve the transformation efficiency of carbonic acid gas, CO
2Per pass conversion can reach more than 75%.Reacting rear material is delivered to synthetic tower separator 2 by the mouth of pipe 19.
The high capacity tray that synthetic tower column plate 18 of the present invention adopts has improved gas in the tower-liquid contact interface greatly, has accelerated the speed of reaction of first ammonium, definitely prevents the back-mixing of solution in the tower simultaneously.
For the medium-sized factory that two urea synthesizers are arranged, then can newly not add first urea synthesizer 1, can utilize wherein one to transform, increase a vertical carbamate condenser and replace the bottom first ammonium conversion zone of first urea synthesizer 1 (as newly adding) to get final product.
Owing to adopted synthetic tower separator 2, isolate the bottom that rich oxygen containing gas phase imports stripping tower 3, add to CO thereby make
2Oxygen in the gas by first urea synthesizer 1, synthetic tower separator 2, stripping tower 3 and second urea synthesizer 4, plays all high-tension apparatuses of the anticorrosion high-pressure system of passivation and the effect of pipeline successively.
Because the lining and the tubulation of first urea synthesizer (1), synthetic tower separator (2) and (3) three high-tension apparatuses of stripping tower that increase all adopt OOCr
25Ni
22Mo
2Material, and the gas that adds stripping tower 3 bottoms is rich oxygen containing gas phase, so technology of the present invention will be the anticorrosion CO that is added to
2Oxygen amount in the charging (adding with air) reduces to 0.25～0.3% by original 0.5%, thereby improve the purity of carbonic acid gas, raising in order to carbon dioxide conversion, and can guarantee the safety in production (because of former process tail gas is an inflammable-explosive gas, domestic took place more than 20 blast accident) of factory.
Compare with existing aqueous solution recycle to extinction Technology, the advantage and the positively effect of novel process of the present invention are as follows:
1. obvious effect of increasing production.The present invention increases by three high-tension apparatuses such as first urea synthesizer 1, synthetic tower separator 2 and stripping tower 3 in the high-pressure system of existing aqueous solution complete circling urea technology, and former urea synthetic tower is made second urea synthesizer 4, forms new high tension loop.Can be according to the different requirements of factory, the throughput of production equipment high tension loop is increased by 30～100%, also promptly adopt method of the present invention can make the throughput of the small-sized urea plant of China increase to 500 tons/day, the throughput of medium-sized urea plant increases to 1000 tons/day.
2. energy conservation and consumption reduction effects is remarkable, steam particularly, and the former aqueous solution recycle to extinction of the consumption rate of water coolant technology reduces significantly.In the technology of the present invention, the reaction heat by-product 0.8～0.9MPaG low-pressure steam owing to utilize the first ammonium in high-pressure system is used for the subsequent handling heating installation and makes thermal source.After the first urea synthesizer fluid is decompressed to 14.5～15.5MpaG, go out first ammonium and the superfluous ammonia that major part does not get transformed into urea in the stripping tower decomposition and separation, the gas that decomposition and separation goes out directly deliver to second urea synthesizer and former in press absorption system to send here the liquid cooling of first ammonium coagulate reaction and change into urea.Like this, the carbon dioxide conversion of whole high-pressure system can reach 70～72%, and the load that press to decompose absorption system in former is reduced greatly, drops to original about 50%.Therefore, the consumption of steam and water coolant reduces significantly.As simultaneously the follow-up unit of urea plant being eliminated the transformation of bottleneck, reduction ammonia consumption and decontamination, consumption indicators is relatively as table 1 before and after then transforming.
Consumption indicators is relatively before and after table 1 aqueous solution complete circling urea plant modification:
| Project | Unit | Small-sized before transforming/medium-sized | After the transformation |
| Ammonia | Ton | ????0.6/0.585 | ????0.57 |
| Carbonic acid gas | Ton | ????0.78/0.77 | ????0.75 |
| Steam | Ton | ????1.5/1.35 | ????0.9 |
| Electricity | Degree | ????155/150 | ????135 |
| Water coolant | Ton | ????165/150 | ????120 |
From table 1 data as seen, with high-pressure system new energy-saving and production-increase process of the present invention former aqueous solution complete circling urea device is transformed, again in conjunction with the transformation that reduces ammonia consumption and decontamination, its energy conservation and consumption reduction effects is remarkable, add significantly effect of increasing production, to bring huge economic benefit to factory, and good social benefit will be arranged.
3. because the bottom of first urea synthesizer 1 is a first ammonium reaction zone, be provided with eddy flow plate and gas distributor,, enter the tubulation section again after reaching temperature of reaction as early as possible to accelerate the speed of reaction of first ammonium at lower tube box.Because the gas distributor of special construction not only can the uniformly distributing gas-liquid enter tubulation, also can make part first ammonium liquid produce internal recycle, improve and accelerate the speed of mass transfer and heat transfer, the gas-liquid that has solved horizontal carbamate condenser is up hill and dale distributed a difficult problem.
4. the expense of Gai Zaoing is low.Because generating, reaction of first ammonium and urea all in first urea synthesizer 1, finishes, two combine into one also to be about to the carbamate condenser and first urea synthesizer, therefore, can reduce the end socket (band manhole) of two high-tension apparatuses, and can simplify pipe arrangement, thereby can reduce the investment of transformation.Technology newly added equipment of the present invention is few, the device fabrication difficulty is little, material easily solves, but equipment layout is installed simple, as to need not high-rise frame, by-product low-pressure steam pressure height and self balance, and the transformation stage does not influence the ordinary production of factory's original device.Improvement expenses is low, only is equivalent to 30～40% of newly-built equal scale plant investment.
Rise steadily and under the low situation of urea price in China joined WTO and domestic energy prices, the middle-size and small-size urea plant of China, if do not change the backward looks of tradition, reduce production costs, form economic scale, thoroughly solve environmental pollution, continue to survive with being difficult in the fierce domestic and international market competition.Adopting the technology of the present invention to carry out the energy-saving and production-increase transformation is the task of top priority, so the present invention has popularizing application prospect widely at home.
Description of drawings
Fig. 1 water solution all-circulation aquadrate high pressure system energy-saving and production-increasing process schema of the present invention
Fig. 2 first urea synthesizer structural representation of the present invention
Below in conjunction with accompanying drawing technology of the present invention is described further.
As shown in Figure 1: in the flow process of the present invention, after unstripped gas carbonic acid gas 5 (oxygen level in the carbon dioxide is 0.25～0.3%) and liquefied ammonia 6 all boost to 20MPaG, enter the bottom of first urea synthesizer 1 in the lump, in order to keep the thermal equilibrium of first urea synthesizer 1, remove part first ammonium reaction heat at first ammonium reaction zone, with the low-pressure steam of this heat by-product 0.8～0.9MPaG.Pressure by control by-product low-pressure steam is controlled the reacting weight of first ammonium, thereby controls the temperature of first urea synthesizer 1.The NH of first urea synthesizer, 1 charging
3/ CO
2Molecular ratio is 3.6～3.8, H
2O/CO
2Molecular ratio is 0, and working pressure is 20～21MPaG, and service temperature is 188～190 ℃, CO
2Per pass conversion can reach more than 75%.
The cat head discharging of first urea synthesizer 1 promptly contains the gas-liquid mixture of urea, first ammonium, water, superfluous ammonia and small amounts of inert gas, delivers to synthetic tower separator 2 and carries out gas-liquid separation, and temperature, pressure in the synthetic tower separator 2 are consistent with synthetic tower 1.The isolated liquid that contains urea, first ammonium, water, superfluous ammonia in synthetic tower separator 2 bottoms is delivered to the top of stripping tower 3 by Liquid level adjusting valve.And be decompressed to the bottom that 14.5～15.5MPaG delivers to stripping tower 3 by pressure controlled valve from the oxygen containing gas phase of synthetic tower separator 2 isolated richnesses.Stripping tower 3 is the falling film type well heater, and shell-side is with 2.2～2.4MPaG middle pressure steam heating, goes out first ammonium and the superfluous ammonia that major part in first urea synthesizer, 1 fluid does not get transformed into urea with decomposition and separation.Stripping tower 3 fluids are controlled at 200～205 ℃, deliver to after being decompressed to 1.7～1.8MPaG and press decomposing system in former.Stripping tower 3 is given vent to anger and is contained ammonia, carbonic acid gas, water and rich oxygen containing rare gas element, with the first ammonium liquid 7 that former one section absorption tower is come, delivers to the bottom of second urea synthesizer 4 together.This tower charging NH
3/ CO
2Molecular ratio is 4.2～4.5, H
2O/CO
2Molecular ratio is 1.3～1.5, and working pressure is 14.5～15.5MPaG, and service temperature is 185～188 ℃, CO
2Per pass conversion can reach 58～60%.The fluid 8 of second urea synthesizer 4 is delivered to the former middle decomposing system of pressing in the lump with stripping tower 3 fluids after being decompressed to 1.7～1.8MPaG.The rich oxygen containing part gas phase 9 of cat head is delivered to the bottom of pressing decomposition heater in former after by the restriction orifice decompression and is made the passivation rot-resistant and add oxygen source, aims at the air compressor of this equipment oxygenation thereby can stop using.Whole high-pressure system CO
2Transformation efficiency can reach 70～72%.
Embodiment
With method of the present invention domestic existing certain medium-sized aqueous solution complete circling urea device is carried out the energy-saving and production-increase transformation, with throughput by 500 tons/day increase production to 750 tons/day be example, estimate total improvement expenses (comprise operation after the former high-pressure system the elimination bottleneck, reduce the transformation of ammonia consumption and decontamination) about 18,000,000 yuan.Transform annual 8250 ten thousand yuan of the output values (pressing 1100 yuan/ton of urea prices) that increase in back; And save energy and reduce the cost, only consider that the consumption of ammonia, steam and electricity reduces, the urea production cost can reduce by 61 yuan/ton, can reduce total cost every year and reach more than 1,300 ten thousand yuan.Only in the energy-saving and cost-reducing production cost that reduces, less than 2 years be the investment of recyclable transformation, the remarkable in economical benefits of factory.On the other hand, thoroughly eliminated the pollution of the waste liquid of discharging in the process unit, waste gas, not only reduced the ammonia consumption, and good social benefit is arranged environment.
Claims (4)
1, a kind of aqueous solution complete circling urea device high-pressure system new energy-saving and production-increase process includes first urea synthesizer (1), synthetic tower separator (2), stripping tower (3) and second urea synthesizer (4), it is characterized in that:
(1) increases by one first urea synthesizer (1), this equipment is divided into first ammonium pre-reaction zone (10), first ammonium reaction zone (11) and urea and generates district's (12) three parts, only at bottom charging feed liquefied ammonia and carbonic acid gas, at first ammonium reaction zone (11), utilize first ammonium reaction heat by-product 0.8～0.9MPaG low-pressure steam, the discharging of synthetic tower (1), the gas-liquid mixture that promptly contains urea, first ammonium, water, superfluous ammonia and small amounts of inert gas is sent into synthetic tower separator (2);
(2) increase a synthetic tower separator (2), the discharging at first urea synthesizer (1) top is carried out gas-liquid separation at synthetic tower separator (2), then, the isolated liquid that contains urea, first ammonium, water, superfluous ammonia in bottom is decompressed to the top that 14.5～15.5MpaG delivers to stripping tower (3), isolated gas promptly contains little ammonia, carbonic acid gas and rich oxygen containing rare gas element and is decompressed to the bottom that 14.5～15.5MPaG delivers to stripping tower (3), as passivation rot-resistant oxygen source;
(3) increase a stripping tower (3), the fluid of synthetic tower separator (2) is decompressed to 14.5～15.5MPaG through Liquid level adjusting valve, enter the top of stripping tower (3), behind packing layer, enter the falling film type well heater, liquid dispenser is adopted on the tubulation top, make the liquid uniformly distributing and be membranaceous from top to bottom and flow along the tubulation inwall, shell-side is with the steam heating of 2.2～2.4MPaG, under high pressure decomposition and separation goes out first ammonium and the superfluous ammonia that major part does not get transformed into urea, stripping tower (3) fluid is decompressed to 1.7～1.8MpaG and delivers to the former middle decomposing system of pressing, stripping tower (3) is given vent to anger and is contained ammonia, carbonic acid gas, water and rich oxygen containing rare gas element enter the bottom of second urea synthesizer (4);
(4) change former urea synthetic tower reduced pressure operation into second urea synthesizer (4), the first ammonium liquid of former M.P. absorber boosts to 14.5～15.5MPaG through former one section first ammonium pump, give vent to anger with stripping tower (3) and to enter the bottom of second urea synthesizer (4) in the lump, the working pressure of synthetic tower (4) is reduced to 14.5～15.4MPaG, 185～188 ℃ of service temperatures, charging NH
3/ CO
2Molecular ratio is 4.2～4.5, H
2O/CO
2Molecular ratio is 1.4～1.5, and the service temperature of synthetic tower (4) feeds a small amount of CO by the rate of decomposition of adjusting stripping tower (3) with in its bottom
2Realize, the fluid of second urea synthesizer (4) is decompressed to 1.7～1.8MPaG and stripping tower (3) fluid enters the former middle decomposing system of pressing in the lump, and the rich oxygen containing part gas phase in second urea synthesizer (4) top is decompressed to 1.8MPaG by restriction orifice and delivers to the former middle bottom of decomposition heater of pressing as the anticorrosion required oxygen of this heating installation passivation.
2, by the described aqueous solution complete circling urea of claim 1 device high-pressure system new energy-saving and production-increase process, it is characterized in that, first urea synthesizer (1) is divided into first ammonium pre-reaction zone (10), first ammonium reaction zone (11) and urea generate district's (12) three parts, reaction of first ammonium and urea generate all to be finished in first urea synthesizer (1), raw materials ammonia and carbonic acid gas are sent into from the bottom by the mouth of pipe (13) and (14) respectively, be provided with eddy flow plate (15) and gas distributor (16) in first ammonium pre-reaction zone (10), to accelerate mass transfer and rate of heat transfer, make reactant reach temperature of reaction as early as possible, and the first ammonium liquid that reaction is generated forms internal recycle in this zone, the gas-liquid uniformly distributing goes into to be provided with first ammonium reaction zone (11) the continuation reaction of heat transfer tubulation (17) then, utilize first ammonium reaction heat by-product 0.8～0.9MPaG low-pressure steam, and with the reacting weight of vapor pressure control first ammonium, keep the thermal equilibrium in the tower, in urea generates district (12), high capacity tray (18) is set, with well distributed gas phase, the interior liquid in increase gas-to-liquid contact interface and absolute anti-zone here is owing to back-mixing takes place in the severe difference, and reacting rear material is delivered to synthetic tower separator (2) by the mouth of pipe (19).
3, by the described aqueous solution complete circling urea of claim 1 device high-pressure system new energy-saving and production-increase process, the lining and the tubulation of wherein said first urea synthesizer (1), synthetic tower separator (2) and stripping tower (3) all adopt OOCr
25Ni
22Mo
2Material.
4, by the described aqueous solution complete circling urea of claim 1 device high-pressure system new energy-saving and production-increase process, it is characterized in that CO
2Oxygen-adding amount in the charging is 0.25～0.3%.
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|---|---|---|---|
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| CNB021237441A CN1194963C (en) | 2002-06-21 | 2002-06-21 | Water solution all-circulation aquadrate high pressure system energy-saving and production-increasing process |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102816091A (en) * | 2011-06-10 | 2012-12-12 | 安徽省科捷再生能源利用有限公司 | Aqueous solution full-cycle urea energy-saving production process |
| CN103396343A (en) * | 2013-07-09 | 2013-11-20 | 内蒙古鄂尔多斯联合化工有限公司 | Corrosion-resistant method for production process system for carbon dioxide gas stripping of urea |
| CN104159888A (en) * | 2012-01-09 | 2014-11-19 | 塞彭公司 | Process for the synthesis of urea comprising a passivation stream at the stripper bottom |
| CN110500910A (en) * | 2019-08-26 | 2019-11-26 | 华北电力大学 | A kind of caloic decoupling heat exchanger and its caloic decoupling method |
-
2002
- 2002-06-21 CN CNB021237441A patent/CN1194963C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102816091A (en) * | 2011-06-10 | 2012-12-12 | 安徽省科捷再生能源利用有限公司 | Aqueous solution full-cycle urea energy-saving production process |
| CN104159888A (en) * | 2012-01-09 | 2014-11-19 | 塞彭公司 | Process for the synthesis of urea comprising a passivation stream at the stripper bottom |
| US9199926B2 (en) | 2012-01-09 | 2015-12-01 | Saipem S.P.A. | Process for the synthesis of urea comprising a passivation stream at the stripper bottom |
| EP2802559B1 (en) | 2012-01-09 | 2016-03-30 | Saipem S.p.A. | Process for the synthesis of urea comprising a passivation stream at the stripper bottom |
| CN104159888B (en) * | 2012-01-09 | 2017-03-22 | 塞彭公司 | Process for the synthesis of urea comprising a passivation stream at the stripper bottom |
| CN103396343A (en) * | 2013-07-09 | 2013-11-20 | 内蒙古鄂尔多斯联合化工有限公司 | Corrosion-resistant method for production process system for carbon dioxide gas stripping of urea |
| CN110500910A (en) * | 2019-08-26 | 2019-11-26 | 华北电力大学 | A kind of caloic decoupling heat exchanger and its caloic decoupling method |
| CN110500910B (en) * | 2019-08-26 | 2023-09-15 | 华北电力大学 | Thermal mass decoupling method of thermal mass decoupling heat exchanger |
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| Publication number | Publication date |
|---|---|
| CN1194963C (en) | 2005-03-30 |
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