CN100340320C - Method for treating decomposed gas by low resistance vertical calandria type absorptive condenser - Google Patents
Method for treating decomposed gas by low resistance vertical calandria type absorptive condenser Download PDFInfo
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- CN100340320C CN100340320C CNB2005100214020A CN200510021402A CN100340320C CN 100340320 C CN100340320 C CN 100340320C CN B2005100214020 A CNB2005100214020 A CN B2005100214020A CN 200510021402 A CN200510021402 A CN 200510021402A CN 100340320 C CN100340320 C CN 100340320C
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- gaseous mixture
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Abstract
The present invention discloses a method for treating decomposed gas by a low-resistance vertical shell and tube absorptive condenser. Mixed gas is added into a condenser from the top and is assigned to each tube array. Thin solution of ammonium carbamate is also added from the top of the condenser to serve as absorbent. Thus, gas and liquid mixture is form in the tube arrays. During the process that the gas and liquid mixture in the tube arrays flows from top to bottom, part of ammonia and carbon dioxide is absorbed into liquid phase through dissolution and chemical reaction, and discharges dissolving heat and chemical reaction heat which are moved away by temperature adjusting water beside a casing. The present invention has the advantages that the present invention can be operated for flexibly and freely controlling heat load absorbed by two stages, the capacity for adapting to the load change of the device is strong, the absorption capacity is enhanced by more than 50%, condensation heat can be effectively controlled, an absorbing reaction effect in the tubes is reached through adding the absorbent, and pipelines can not be blocked. The technique has a favorable application foreground in capacity enlarging reconstruction of devices of the same class.
Description
Technical field
The present invention relates to a kind of absorption process that contains ammonia and carbon dioxide gas mixture, particularly absorb precondenser and handle the method that contains ammonia and carbon dioxide mix gas with low resistance vertical calandria type.
Technical background
During the branch of urea production process is vented one's spleen, mainly contain ammonia, carbon dioxide, water vapour, also have some noble gases (hereinafter to be referred as gaseous mixture), it is concrete forms with the composition of synthesis reaction solution and decomposition technique parameter and different.Ammonia in the gaseous mixture and carbon dioxide recovery also loop back the method for synthesis procedure, in once the occurring in early days of urea production " hot gas cycle method ", because of the NH of heat
3And CO
2Directly compression easily causes in the gas phase crystallization and technical difficulty such as high temperature compressed and fails to realize industrialization.In the various flow processs of present urea production, (in) the low pressure branch is vented one's spleen all is to absorb ammonia and carbon dioxide with solvent, making becomes non crystallized high concentration first ammonium salt solution and loops back synthesis procedure.Generally need increase certain water yield, so that with NH at the final stage exhausting section
3And CO
2Fully reclaim, and at the previous stage exhausting section, the rare first ammonium liquid that then uses back one-level exhausting section to obtain reclaims the NH that divides in vent one's spleen (being gaseous mixture) as absorbent
3And CO
2, so just can reduce the water yield in the first ammonium liquid, guarantee that the synthesis procedure steam/hydrocarbons ratio is unlikely too high.
NH
3-CO
2-H
2O ternary system gas-liquid phase equilibrium and liquid-solid phase balance are the theoretical foundation of condensation removal process.Utilize gas-liquid phase equilibrium under the certain pressure can determine gentle, the amount of liquid phase of composition of absorption liquid, relevantly studies show that each pressure all exists an optimal point of operation, it is NH
3-CO
2-H
2The turning point of the isobaric saturated line of O ternary system, the solution C O of this point
2Content is the highest, and steam/hydrocarbons ratio is minimum, and therefore, Synthesis conversion one is regularly taken back the least amount of water of synthesis system.And utilize liquid-solid phase balance under the certain pressure can make absorption process is to carry out in the solution district, is that the operating temperature of requirement absorption process is higher than crystallization temperature 10-20 ℃ generally speaking, just can guarantee the absorption process trouble-free operation.
During urea production process such as improvement C method, ACES method, IDR method and water solution total cycling method all are provided with, two sections recovery systems of low pressure come condensation to absorb ammonia and the carbon dioxide that divides in vent one's spleen (being gaseous mixture), and the ammonia vaporizing extract process is provided with the multistage recovery system especially, only has carbon dioxide stripping technology only to adopt low pressure recovery system and exhaust gas recovery system.In all these recovery systems, condensation absorption pattern most cases is the method that adopts the bubbling submergence to absorb, and at low concentration region the method for using packed tower or plate column to absorb is arranged also, and all there is the bigger shortcoming of resistance drop in this type of condensation absorption pattern.Heat of solution and chemical reaction heat for the condensation absorption process have the various method of many formulas, comprise with recirculated water directly cooling off, being used to heat urine etc. with the temperature adjustment water cooling and under elevated pressures (0.45MPa) condensation absorbing state.Generally speaking, all carry out at shell-side by the condensation absorption process in the design, promptly housing and tubulation are all wanted the mordant first ammonium of contact zones liquid medium, and therefore whole equipment all must adopt the higher stainless steel material of grade, thereby causes the high situation of equipment investment.
Domestic relevant enterprise has also adopted precondenser in the circulatory system expands energy, but be parallel on its structure, and does not add follow-up workshop section absorption liquid and make absorbent, promptly stops up after causing equipment to come into operation, and can't continue use.In addition, expansion energy for the circulatory system, more suggestion and discussion are to increase to press, decompose absorption system in the cover, and with direct cooling water absorption replacement temperature adjustment water system, this is all higher with the capital cost that adopts flow process in parallel, and this is unusual difficulty for the heat balance of circulation absorption portion and water yield control, and also remains textual criticism preventing that the crystallization of first ammonium liquid from stopping up.
Summary of the invention
Purpose of the present invention promptly is to overcome the shortcoming of prior art, provide a kind of low resistance vertical calandria type to absorb precondenser and handle the method that contains ammonia and carbon dioxide mix gas, can make condensation heat effectively controlled, and add absorbent and make and reach the absorption reaction effect in the pipe, unlikely again blocking pipe.
Purpose of the present invention is achieved through the following technical solutions: mist adds from the precondenser top, be imported in the precondenser upper tube box, rely on diffusion to be assigned to each tubulation, in this condensation absorption process, added rare first ammonium liquid that follow-up low concentration workshop section returns as absorbent, also add by the precondenser top, and evenly distribute by nozzle, in upper tube box, absorbent is evenly sprayed each tubulation by nozzle, just formed gas-liquid mixture thus in the tubulation, gas-liquid mixture in the tubulation part ammonia and carbon dioxide in top-down flow process are absorbed in the liquid phase by dissolving and chemical reaction, and emit heat of solution and chemical reaction heat, heat of solution and chemical reaction heat are removed by shell-side temperature adjustment water, and temperature adjustment water flows provides energy by circulating pump, and heat is taken away by cooling water in recirculation cooler.
By top narration as can be seen, the present invention has the following advantages: the thermic load that can control two sections absorptions in operation flexibly and comfortably, very strong and absorbability improves more than 50% to the ability of adaptive device load variations, make condensation heat effectively controlled, and add absorbent and make and reach the absorption reaction effect in the pipe, unlikely again blocking pipe, this technology has a good application prospect in the capacity expansion revamping of same device.
Description of drawings
Fig. 1 is a schematic flow sheet of the present invention.
Fig. 2 produces residing position in the urea technique for the present invention in whole C O2 vaporizing extract process.
The specific embodiment
The present invention will be further described below in conjunction with accompanying drawing: as shown in Figure 1, the temperature of coming from rectifying column is 105-112 ℃, contain ammonia about 34%, carbonated about 51%, all the other are imported in the precondenser upper tube box for the gaseous mixture of water vapour, rely on diffusion to be assigned to each tubulation, total concentration is that rare first ammonium liquid of 47-53% is evenly distributed by nozzle, the nozzle spray angle of the rare first ammonium of spray absorbent liquid is 90-120 ° and evenly sprays each tubulation, gas-liquid mixture in the tubulation part ammonia and carbon dioxide in top-down flow process are absorbed in the liquid phase, and emit heat of solution and chemical reaction heat, go out the gas of precondenser, liquid mixture, temperature is controlled to be and is not less than 75 ℃, is imported into the further condensation of the original submergence bubble type of device absorption reactor thermally again and absorbs.Heat of solution and chemical reaction heat are removed by shell-side temperature adjustment water, and temperature adjustment discharge is controlled to be 700-900m3/h, and temperature is 65-75 ℃, allow 5-7.5 ℃ of maximum temperature rise, and temperature adjustment water flows provides energy by circulating pump, and heat is taken away by cooling water in recirculation cooler.Upright shell and tube absorbs the precondenser heat exchanging pipe and uses stainless steel material, and housing uses carbon steel material.
As shown in Figure 2, Fig. 2 is that the present invention is at whole C O
2Vaporizing extract process is produced residing position in the urea technique.
Claims (7)
1. absorb the method that precondenser is handled gaseous mixture with low resistance vertical calandria type, described gaseous mixture is the gaseous mixture that contains ammonia and carbon dioxide, it is characterized in that: gaseous mixture adds from the precondenser top, be imported in the precondenser upper tube box, rely on diffusion to be assigned to each tubulation, in this condensation absorption process, added rare first ammonium liquid that follow-up low concentration workshop section returns as absorbent, also add by the precondenser top, and evenly distribute by nozzle, evenly spray each tubulation, just formed gas-liquid mixture thus in the tubulation, gas-liquid mixture in the tubulation part ammonia and carbon dioxide in top-down flow process are absorbed in the liquid phase by dissolving and chemical reaction, and emit heat of solution and chemical reaction heat, heat of solution and chemical reaction heat are removed by shell-side temperature adjustment water, temperature adjustment water flows provides energy by circulating pump, and the heat that temperature adjustment water is removed is taken away by cooling water in recirculation cooler.
2. the method with low resistance vertical calandria type absorption precondenser processing gaseous mixture according to claim 1, it is characterized in that: upright shell and tube absorbs the precondenser heat exchanging pipe and uses stainless steel material, housing use carbon steel material.
3. the method with low resistance vertical calandria type absorption precondenser processing gaseous mixture according to claim 1, it is characterized in that: temperature adjustment discharge is controlled to be 700-900m3/h, and temperature is 65-75 ℃, allows 5-7.5 ℃ of maximum temperature rise.
4. the method with low resistance vertical calandria type absorption precondenser processing gaseous mixture according to claim 1, it is characterized in that: go out gas, the liquid mixture of precondenser, temperature is controlled to be and is not less than 75 ℃.
5. the method with low resistance vertical calandria type absorption precondenser processing gaseous mixture according to claim 1, it is characterized in that: the spray angle of described nozzle is 90-120 °.
6. the method with low resistance vertical calandria type absorption precondenser processing gaseous mixture according to claim 1 is characterized in that: the gaseous mixture that adds from the precondenser top, to come from rectifying column, and temperature is 105-112 ℃.
7. the method with low resistance vertical calandria type absorption precondenser processing gaseous mixture according to claim 1, it is characterized in that: the rare first ammonium of absorbent liquid total concentration is 47-53%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100214020A CN100340320C (en) | 2005-08-03 | 2005-08-03 | Method for treating decomposed gas by low resistance vertical calandria type absorptive condenser |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100214020A CN100340320C (en) | 2005-08-03 | 2005-08-03 | Method for treating decomposed gas by low resistance vertical calandria type absorptive condenser |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1736531A CN1736531A (en) | 2006-02-22 |
| CN100340320C true CN100340320C (en) | 2007-10-03 |
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|---|---|---|---|
| CNB2005100214020A Active CN100340320C (en) | 2005-08-03 | 2005-08-03 | Method for treating decomposed gas by low resistance vertical calandria type absorptive condenser |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1058704C (en) * | 1996-01-11 | 2000-11-22 | 化学工业部上海化工研究院 | Method for prepn. of urea by carbon dioxide stripping method |
| US20020188157A1 (en) * | 2000-07-04 | 2002-12-12 | Toyo Engineering Corporation | Urea synthesis process and apparatus |
| CN1137882C (en) * | 2001-03-23 | 2004-02-11 | 中国寰球工程公司 | Full-circulating process for preparing urea |
| US20050065374A1 (en) * | 2003-09-19 | 2005-03-24 | Urea Casale S.A. | Carbamate condensation method and unit for carrying out such a method |
-
2005
- 2005-08-03 CN CNB2005100214020A patent/CN100340320C/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1058704C (en) * | 1996-01-11 | 2000-11-22 | 化学工业部上海化工研究院 | Method for prepn. of urea by carbon dioxide stripping method |
| US20020188157A1 (en) * | 2000-07-04 | 2002-12-12 | Toyo Engineering Corporation | Urea synthesis process and apparatus |
| CN1137882C (en) * | 2001-03-23 | 2004-02-11 | 中国寰球工程公司 | Full-circulating process for preparing urea |
| US20050065374A1 (en) * | 2003-09-19 | 2005-03-24 | Urea Casale S.A. | Carbamate condensation method and unit for carrying out such a method |
Non-Patent Citations (1)
| Title |
|---|
| 二氧化碳汽提法尿素装置循环系统改造探讨 茅启昌，周寅义，李勇，大氮肥，第26卷第4期 2003 * |
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| Publication number | Publication date |
|---|---|
| CN1736531A (en) | 2006-02-22 |
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