CN101284771B - Exhaust steam trap and method of use thereof - Google Patents
Exhaust steam trap and method of use thereof Download PDFInfo
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- CN101284771B CN101284771B CN2008100533551A CN200810053355A CN101284771B CN 101284771 B CN101284771 B CN 101284771B CN 2008100533551 A CN2008100533551 A CN 2008100533551A CN 200810053355 A CN200810053355 A CN 200810053355A CN 101284771 B CN101284771 B CN 101284771B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention relates to the utilization of steam, in particular to the utilization of boiler steam during the benzoic acid production process, which provides a dead steam catcher and the application thereof. The dead steam catcher adopts the structure that a steam-water separating valve is arranged at the middle upper part of the dead steam catcher, a steam-water separating disk is arranged at the middle lower part of the dead steam catcher, an steam inlet is formed between the steam-water separating valve and the steam-water separating disk, three steam outlets are formed at the top part ofthe dead steam catcher, and two water outlets are formed at the lower part of the dead steam catcher. The novel energy-saving equipment of the dead steam catcher (for short: boiling boiler) is adopted during the benzoic acid production process to collect the dead steam, which is generated after the toluene in an oxidation column is heated by the saturated boiler steam, so that the pressure of thedead steam is effectively maintained, and the maximum temperature of the dead steam, namely the enthalpy of the dead steam is also maintained, and can be reused for the production system.
Description
Technical field
The present invention relates to the utilization of Boiler Steam in the utilization of steam, particularly production process of benzoic acid, propose a kind of exhaust steam trap and using method.
Background technology
In benzoic production process, main chemical reaction process is the oxidizing reaction of toluene.Before oxidation, need the toluene of normal temperature attitude in the oxidizing tower is warming up to 160～165 ℃.What heat temperature raising used is the saturated Boiler Steam of 0.8Mpa, and vapor temperature reaches 170～175 ℃.Boiler Steam after heat temperature raising uses becomes weary steam, is called for short exhaust steam.Present most of manufacturer this part exhaust steam only as heating, add daily life vapour such as hot water.With regard to making steam can not get more abundant effective utilization, cause the significant wastage of the energy like this with high enthalpy value for this reason.
Summary of the invention
The purpose of this invention is to provide a kind of energy-efficient equipment, a kind of use flow process of weary steam is provided; Make weary steam obtain utilizing fully efficiently with high enthalpy value.
For achieving the above object, technical scheme of the present invention is as follows:
The weary vapor collection of in benzoic production process, using a kind of new energy-efficient equipment-exhaust steam trap (be called for short: pot boils) that saturated Boiler Steam is become behind the toluene heat temperature raising in to oxidizing tower, keep the top temperature of the pressure of weary steam and weary steam promptly to keep the enthalpy of weary steam effectively, be used for production system once more.
Exhaust steam trap of the present invention, be to be provided with the carbonated drink seperating vale in the middle and upper part of exhaust steam trap, be provided with the carbonated drink separator disk in the middle and lower part of exhaust steam trap, between carbonated drink seperating vale and carbonated drink separator disk, be provided with steam inlet, be provided with three steam outlets at the top of exhaust steam trap, be provided with two water outlets in the bottom of exhaust steam trap.
Exhaust steam trap diameter 1400～1800mm of the present invention, long 6000～8000mm.
Exhaust steam trap of the present invention is in the production system of sealing, the weary steam that the saturated Boiler Steam of 0.8Mpa is become after to the toluene heat temperature raising in the oxidizing tower enters exhaust steam trap by steam inlet d, vapor pressure in exhaust steam trap reaches 0.2Mpa～0.3Mpa, when temperature is 133 ℃～143 ℃, be transported to employed equipment by the first steam outlet b1, the second steam outlet b2, the 3rd steam outlet b3; Water of condensation in the exhaust steam trap outputs to employed equipment by the first water outlet c, the second water outlet M.
For simplicity, the first following steam outlet b1, the second steam outlet b2, the 3rd steam outlet b3 use air outlet (or steam outlet) b1, b2 and b3 summary respectively, and the first water outlet c and the second water outlet M replace with water outlet c and M respectively.
The using method of exhaust steam trap of the present invention, when the toluene temperature in the oxidizing tower reached 160～165 ℃, the water of condensation in the exhaust steam trap outputed to by water outlet M that cooling but uses in the oxidizing tower of phenylformic acid production system.This moment, the heating coil temperature was 160 ℃～175 ℃, and condensate temperature is: 90～95 ℃.
When the condensate temperature in the described exhaust steam trap is 90～95 ℃, by water outlet c water of condensation is transported to the Sodium Benzoate production system and uses for phenylformic acid+sodium hydroxide N-process.
The vapor pressure of the first half reaches 0.2Mpa～0.3Mpa in the described exhaust steam trap, when temperature is 133 ℃～143 ℃, closes air outlet b2, b3, is transported to the phenylformic acid production system by steam outlet b1 and uses for the drying process of tail gas adsorber.
Described vapor pressure on exhaust steam trap top reaches 0.2Mpa～0.3Mpa, temperature: close air outlet b1, b3 in the time of 133 ℃～143 ℃, be transported to commercial benzene formic acid production system by steam outlet b2 and use for drying process.
Described vapor pressure on exhaust steam trap top reaches 0.2Mpa～0.3Mpa, temperature: close air outlet b1, b2 in the time of 133 ℃～143 ℃, be transported to the Sodium Benzoate production system by steam outlet b3 and use for phenylformic acid+sodium hydroxide N-process.
As the effect of water coolant the toluene temperature in the oxidizing tower is stayed relatively constant at about 160 ℃ at this water of condensation that adopts exhaust steam trap, not only stablized production status but also saved saturated Boiler Steam greatly, the valve regulated operating frequency that has reduced operator has simultaneously improved working efficiency.Only saving coal-fired every year in production reality is 2592 tons, saves the amount of money and reaches: 155.5 ten thousand yuan, and saves energy 220KW/h.Reduce the slag emission amount: reach 130 tons every year, reduce sulfurous gas, smoke discharge amount and reach 20,000 mark cubic meters every year.Guaranteed the realization of target for energy-saving and emission-reduction.
Description of drawings
Fig. 1: exhaust steam trap synoptic diagram of the present invention;
Fig. 2: exhaust steam trap vertical view of the present invention.
Wherein: d is a steam inlet, and a is a relief valve port, and b1-3-is a steam outlet, and c, m are water outlet, and f is a sewage draining exit, and e is the carbonated drink seperating vale, and g is the carbonated drink separator disk.
Embodiment
The present invention is described in further detail below in conjunction with accompanying drawing:
Adopt equipment as shown in Figure 1, concrete mode of connection is as follows:
1, inlet mouth d is connected with the outlet of oxidizing tower heating tube;
2, a mouth device safety valve;
3, steam outlet b1 is connected with the dry pipeline of phenylformic acid production system tail gas adsorber, and the dry pipeline of steam outlet b2 and commercial benzene formic acid production system is connected, and is connected with the operation vapour line in steam outlet b3 and the Sodium Benzoate production system;
4, the heating pipeline in water outlet c, m and the oxidizing tower is connected, and is connected with the operation water pipeline in the Sodium Benzoate production system;
5, sewage draining exit f is connected with external blowdown pipeline.
6, the carbonated drink seperating vale is installed in the middle and upper part of exhaust steam trap tank body.When weary steam reaches certain pressure with seperating vale jack-up, make weary steam constantly enter tank body top, again seperating vale is depressed when weary steam reaches certain pressure, at this moment vapor pressure, the temperature in the exhaust steam trap can be allocated use when each production station needs.So far carbonated drink seperating vale do action under the effect of weary steam.
7, the carbonated drink separator disk is installed in the middle and lower part of exhaust steam trap tank body.Enter to concentrate behind water of condensation contained in the weary steam of exhaust steam trap enters into the exhaust steam trap tank body by the carbonated drink separator disk the bottom by steam inlet and use.The carbonated drink separator disk plays the effect of vapour, water sepn.
In conjunction with Fig. 2: the exhaust steam trap applicating flow chart
Embodiment 1: toluene is squeezed into oxidizing tower, open saturated boiler steam valve, use the saturated Boiler Steam of 0.8Mpa to give the toluene heat temperature raising of normal temperature attitude.Reach 120 ℃ of beginning airy in the toluene temperature and continue to be warming up to 160 ℃ simultaneously, close saturated boiler steam valve then, the weary steam that the saturated Boiler Steam of using for the toluene heat temperature raising this moment has become is all collected by exhaust steam trap (be called for short: pot boils).Close air outlet b1-3, close bottom water outlet c, open the M-water outlet of bottom, with temperature is that 90～95 ℃ water of condensation is transported in the oxidizing tower in the former coil pipe to the toluene heating, cooling has had the toluene of 160 ℃～175 ℃ of temperature, regulates the water of condensation valve opening at any time the temperature of this toluene is stayed relatively constant at about 160 ℃.
Embodiment 2: the vapor pressure at exhaust steam trap (be called for short: the pot boils) first half reaches 0.2Mpa～0.3Mpa, temperature: in the time of 133 ℃～143 ℃, close air outlet b2, b3, close water outlet c, M, be transported to the phenylformic acid production system by the b1-steam outlet and use for the drying process of tail gas adsorber.
Embodiment 3: the vapor pressure on exhaust steam trap (be called for short: pot boils) top among the embodiment 2 reaches 0.2Mpa～0.3Mpa, temperature: close air outlet b1, b3 in the time of 133 ℃～143 ℃, close water outlet c, M, be transported to commercial benzene formic acid production system by the b2-steam outlet and use for drying process.
Embodiment 4: the vapor pressure on exhaust steam trap (be called for short: pot boils) top among the embodiment 2 reaches 0.2Mpa～0.3Mpa, temperature: in the time of 133 ℃～143 ℃, close air outlet b1, b2, close water outlet c, M, be transported to the Sodium Benzoate production system by the b3-steam outlet and use for phenylformic acid+sodium hydroxide N-process.
Embodiment 5: among the embodiment 2 at the c-water outlet of opening exhaust steam trap (be called for short: boil pot) bottom, close air outlet b1-3, closing the M-water outlet, is that 90～95 ℃ water of condensation is transported to the Sodium Benzoate production system and uses for phenylformic acid+sodium hydroxide N-process with temperature.
The present invention is save energy not only, and reduces the discharging of sulfurous gas and flue dust.
Exhaust steam trap and using method that the present invention proposes, be described by embodiment, person skilled obviously can be changed or suitably change and combination making method as herein described in not breaking away from content of the present invention, spirit and scope, realizes the technology of the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as being included in spirit of the present invention, scope and the content.
Claims (8)
1. exhaust steam trap, it is characterized in that being provided with the carbonated drink seperating vale in the middle and upper part of exhaust steam trap, be provided with the carbonated drink separator disk in the middle and lower part of exhaust steam trap, between carbonated drink seperating vale and carbonated drink separator disk, be provided with steam inlet, be provided with three steam outlets at the top of exhaust steam trap, be provided with two water outlets in the bottom of exhaust steam trap.
2. exhaust steam trap as claimed in claim 1 is characterized in that described exhaust steam trap diameter 1400～1800mm, long 6000～8000mm.
3. the using method of claim 1 exhaust steam trap, it is characterized in that the weary steam that becomes after saturated Boiler Steam is to the toluene heat temperature raising in the oxidizing tower enters exhaust steam trap by steam inlet (d), vapor pressure in exhaust steam trap reaches 0.2Mpa～0.3Mpa, when temperature is 133 ℃～143 ℃, be transported to employed equipment by first steam outlet (b1), second steam outlet (b2), the 3rd steam outlet (b3); Water of condensation in the exhaust steam trap outputs to employed equipment by first water outlet (c), second water outlet (M).
4. the using method of exhaust steam trap as claimed in claim 3, it is characterized in that closing when the interior condensate temperature of described exhaust steam trap is 90～95 ℃ first steam outlet (b1), second steam outlet (b2) and the 3rd steam outlet (b3), close second water outlet (M), by first water outlet (c) water of condensation is transported to the Sodium Benzoate production system and uses for N-process.
5. the using method of exhaust steam trap as claimed in claim 3, it is characterized in that closing when the interior toluene temperature when in the oxidizing tower of described exhaust steam trap reaches 160 ℃～165 ℃ first steam outlet (b1), second steam outlet (b2) and the 3rd steam outlet (b3), close first water outlet (c), water of condensation is but used by the interior cooling of oxidizing tower that second water outlet (M) is transported to the phenylformic acid production system.
6. the using method of exhaust steam trap as claimed in claim 3, the vapor pressure that it is characterized in that the first half in the described exhaust steam trap reaches 0.2Mpa～0.3Mpa, when being 133 ℃～143 ℃, temperature closes first water outlet (c) and second water outlet (M), close second steam outlet (b2) and the 3rd steam outlet (b3), be transported to the phenylformic acid production system by first steam outlet (b1) and use for the drying process of tail gas adsorber.
7. the using method of exhaust steam trap as claimed in claim 3, it is characterized in that described vapor pressure on exhaust steam trap top reaches 0.2Mpa～0.3Mpa, when temperature is 133 ℃～143 ℃, close first water outlet (c) and second water outlet (M), close first steam outlet (b1) and the 3rd steam outlet (b3), be transported to commercial benzene formic acid production system by second steam outlet (b2) and use for drying process.
8. the using method of exhaust steam trap as claimed in claim 3, it is characterized in that described vapor pressure on exhaust steam trap top reaches 0.2Mpa～0.3Mpa, when temperature is 133 ℃～143 ℃, close first water outlet (c) and second water outlet (M), close first steam outlet (b1) and second steam outlet (b2), be transported to the Sodium Benzoate production system by the 3rd steam outlet (b3) and use for N-process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100533551A CN101284771B (en) | 2008-05-30 | 2008-05-30 | Exhaust steam trap and method of use thereof |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100533551A CN101284771B (en) | 2008-05-30 | 2008-05-30 | Exhaust steam trap and method of use thereof |
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| CN101284771A CN101284771A (en) | 2008-10-15 |
| CN101284771B true CN101284771B (en) | 2011-04-27 |
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| CN2008100533551A Expired - Fee Related CN101284771B (en) | 2008-05-30 | 2008-05-30 | Exhaust steam trap and method of use thereof |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101508641B (en) * | 2009-03-20 | 2012-12-12 | 天津市东大化工有限公司 | Applied technology for realizing circular economy industrial chain in benzoic acid purification production process |
| CN102861542A (en) * | 2012-09-27 | 2013-01-09 | 天津东大化工集团有限公司 | Methylbenzene oxidation tower in 10000-tone level benzoic acid production |
| CN110922323B (en) * | 2019-11-27 | 2024-07-02 | 天津东大化工集团有限公司 | Thermal-electric coupling high-efficiency energy-saving emission-reduction process for producing benzoic acid by continuous catalytic oxidation of toluene |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2285676Y (en) * | 1996-12-27 | 1998-07-08 | 枣庄市立医院 | Steam purifying and ammonia removing device |
| CN2423020Y (en) * | 2000-05-08 | 2001-03-14 | 湖南大学 | Reactor of device for preparing phenol from benzoic acid |
-
2008
- 2008-05-30 CN CN2008100533551A patent/CN101284771B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2285676Y (en) * | 1996-12-27 | 1998-07-08 | 枣庄市立医院 | Steam purifying and ammonia removing device |
| CN2423020Y (en) * | 2000-05-08 | 2001-03-14 | 湖南大学 | Reactor of device for preparing phenol from benzoic acid |
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