CN203741248U - Improved oxidation reaction and tail gas adsorption device for synthesizing glyoxylic acid - Google Patents
Improved oxidation reaction and tail gas adsorption device for synthesizing glyoxylic acid Download PDFInfo
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- CN203741248U CN203741248U CN201420118230.3U CN201420118230U CN203741248U CN 203741248 U CN203741248 U CN 203741248U CN 201420118230 U CN201420118230 U CN 201420118230U CN 203741248 U CN203741248 U CN 203741248U
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- HHLFWLYXYJOTON-UHFFFAOYSA-N glyoxylic acid Chemical compound OC(=O)C=O HHLFWLYXYJOTON-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 230000002194 synthesizing effect Effects 0.000 title claims abstract description 18
- 238000007254 oxidation reaction Methods 0.000 title abstract description 14
- 238000001179 sorption measurement Methods 0.000 title description 2
- 238000010521 absorption reaction Methods 0.000 claims abstract description 94
- 239000007788 liquid Substances 0.000 claims abstract description 47
- 238000006243 chemical reaction Methods 0.000 claims abstract description 43
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical group O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000011084 recovery Methods 0.000 claims abstract description 25
- 238000001816 cooling Methods 0.000 claims abstract description 13
- 229910017604 nitric acid Inorganic materials 0.000 claims description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- 230000001590 oxidative effect Effects 0.000 claims description 27
- 239000000498 cooling water Substances 0.000 claims description 12
- 230000007797 corrosion Effects 0.000 claims description 8
- 238000005260 corrosion Methods 0.000 claims description 8
- 239000002826 coolant Substances 0.000 claims description 7
- 238000012856 packing Methods 0.000 claims description 5
- 239000012266 salt solution Substances 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- 238000007789 sealing Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 72
- 239000002994 raw material Substances 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 4
- 230000006872 improvement Effects 0.000 abstract description 3
- 239000002912 waste gas Substances 0.000 abstract description 3
- 150000001875 compounds Chemical class 0.000 abstract 1
- 238000000034 method Methods 0.000 description 26
- 230000008569 process Effects 0.000 description 18
- 230000003647 oxidation Effects 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 9
- 239000004743 Polypropylene Substances 0.000 description 7
- 239000007791 liquid phase Substances 0.000 description 6
- ZNZYKNKBJPZETN-WELNAUFTSA-N Dialdehyde 11678 Chemical compound N1C2=CC=CC=C2C2=C1[C@H](C[C@H](/C(=C/O)C(=O)OC)[C@@H](C=C)C=O)NCC2 ZNZYKNKBJPZETN-WELNAUFTSA-N 0.000 description 5
- 238000012545 processing Methods 0.000 description 5
- 238000007086 side reaction Methods 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000007664 blowing Methods 0.000 description 3
- 125000003178 carboxy group Chemical group [H]OC(*)=O 0.000 description 3
- 235000006408 oxalic acid Nutrition 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- -1 papermaking Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 2
- 230000032683 aging Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229920001155 polypropylene Polymers 0.000 description 2
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- 230000001360 synchronised effect Effects 0.000 description 2
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- 229910000831 Steel Inorganic materials 0.000 description 1
- 150000008065 acid anhydrides Chemical class 0.000 description 1
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- 239000003905 agrochemical Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
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- VZCYOOQTPOCHFL-UPHRSURJSA-N maleic acid Chemical compound OC(=O)\C=C/C(O)=O VZCYOOQTPOCHFL-UPHRSURJSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
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- 239000007800 oxidant agent Substances 0.000 description 1
- 238000006385 ozonation reaction Methods 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
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- 238000012827 research and development Methods 0.000 description 1
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- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to an improved oxidation reaction and tail gas absorption device for synthesizing glyoxylic acid. The device is characterized by comprising a reaction kettle, a tail gas condenser, an absorption tower, an absorption liquid cooler and an absorption liquid circulating lamp, wherein the reaction kettle comprises an air inlet pipe and a feed pipe; the tail gas condenser is arranged at the tail gas outlet of the reaction kettle; the tail gas condenser is communicated with the absorption tower; the absorption tower and the absorption liquid cooler form a cooling circulating loop through the absorption liquid circulating pump. Many-sided improvements are conducted on the traditional device, and devices or compounds of an air blower, the tail gas condenser, the absorption liquid cooler, an air distribution pipe and a liquid raw material distribution pipe and the like are additionally arranged, so that the oxidation reaction effect is improved, the raw material recovery rate is increased, the product yield is obviously increased, the nitric acid unit consumption is obviously reduced, and standard emission of waste gas is realized.
Description
Technical field
The utility model relates to a kind of oxidizing reaction of modified form synthesizing glyoxalic acid and the device that tail gas absorbs, and belongs to technical field of chemical.
Background technology
Oxoethanoic acid is a kind of important fine chemical material and intermediate, is widely used in the synthetic field of the light industrial goods such as spices, medicine, agricultural chemicals, papermaking, coating, paint, leather and foodstuff additive.At present, industrial more conventional chemical synthesis process mainly contains three kinds of oxalic dialdehyde nitric acid oxidation methods, acid by electrolytic reduction of oxalic method, toxilic acid (acid anhydride) Ozonation.Wherein, oxalic dialdehyde nitric acid oxidation method, with its lower cost with compared with proven technique, becomes the Synthetic Methods of Glyoxalic Acid that domestic and international manufacturer generally adopts.
Oxalic dialdehyde nitric acid oxidation method is under the katalysis of the auxiliary agents such as hydrochloric acid, with nitric acid as oxidant selective oxidation oxalic dialdehyde, generates principal product oxoethanoic acid, and by-product oxalic acid.Reaction principle is as follows:
Main reaction equation is:
3CHO-CHO + 2HNO
3 → 3CHO-COOH + 2NO↑ + H
2O ①
Inevitably because oxoethanoic acid is further oxided, there is side reaction, generate a certain amount of by product oxalic acid simultaneously.Side reaction equation is:
3CHO-COOH + 2HNO
3 → 3HOOC-COOH + 2NO↑ + H
2O ②
The synthetic method of current main flow is the introducing air (O containing approximately 21% also
2) participate in reaction, by airborne O
2nO is oxidized to NO
2, NO
2further by water absorption reaction, generate nitric acid or nitrous acid and become the oxygenant of recoverable, solve problem of environmental pollution simultaneously.Mainly there is following reaction in this conversion process:
2NO + O
2 ＝2NO
2 ③
3NO
2 + H
2O ＝ 2HNO
3 + NO ④
4NO
2 + O
2 + 2H
2O ＝ 4HNO
3 ⑤
By literature search with to main manufacturer of the same trade investigation, we find, existing and realized at present industrialized oxidation reaction apparatus and device for absorbing tail gas and mainly contain following common feature:
(1) oxidation furnaces is lass lining stills for air blowing, and structure is too simple, can not meet the needs of oxidizing reaction, can not adapt to well the requirements such as optimization of process conditions.
(2) tail gas absorption equipment adopts packing tower water to absorb mostly, and minority producer is with alkali liquor absorption device, and with recovery oxygenant nitric acid reduction of discharging, but because device level is uneven, part producer is the target of unrealized qualified discharge also.
(3) common feature of oxidation furnaces and absorption equipment is, equipment is too simplified, simplification, according to the principle of the characteristic of technique self and oxidizing reaction and tail gas recycle improvement, do not carry out appropriate design exploitation, generally adopt general-purpose equipment but not specific equipment.
Mainly there is following defect in above-mentioned existing apparatus:
Although A has introduced air and participated in reaction, this is mainly in tail gas absorption process, NO being oxidized to NO
2reducing water absorption difficulty introduces, the introducing of air does not cause much Beneficial Effects to oxidizing reaction itself, from source, do not make full use of the oxygenant of overflowing from still and realize energy-saving and emission-reduction, thereby tail gas generation is larger, to environmental protection, has caused very large pressure.
B, most equipment flowsheet that connects induced draft fan at absorption tower end that adopts, reactor and absorption tower whole system are moved under negative pressure, this can cause the rapid, high volume of sour gas in stills for air blowing to run off, and negative pressure is also unfavorable for that the water of gas absorbs, and makes desorb aggravation, makes the rate of recovery degradation of nitric acid, the concentration that reclaims nitric acid is also rarer, cause absorption liquid total amount to strengthen, apply mechanically rear redundance and have to process and discharge, be unfavorable for energy-saving and emission-reduction.
C, the oxidizing reaction temperature conventionally adopting are 50-80 ℃, the gas temperature of being extracted out by negative pressure is up to 40-60 ℃, do not take cooling measure directly to enter absorption system, exothermic heat of reaction in while absorption process, make absorption temperature higher, absorb treatment effect not good, be unfavorable for improving raw materials recovery rate and reduction of discharging, and system operation is stable not, and the phenomenon of discharge beyond standards happens occasionally.
Based on above reason, be badly in need of the new method for treating tail gas of research and development or optimize oxidizing process condition and support equipment thereof.
Summary of the invention
In order to address the aforementioned drawbacks and deficiency, the utility model provides a kind of oxidizing reaction of modified form synthesizing glyoxalic acid and the device that tail gas absorbs, and not only can improve oxidizing reaction effect and raw materials recovery rate, and product yield is significantly improved, nitric acid unit consumption obviously declines, and has realized waste gas qualified discharge.Described technical scheme is as follows:
The utility model embodiment provides a kind of oxidizing reaction of modified form synthesizing glyoxalic acid and the device that tail gas absorbs, it is characterized in that, this device comprises: reactor, tail gas condenser, absorption tower, absorption liquid water cooler, absorption liquid recycle pump, described reactor comprises inlet pipe and feed-pipe, the tail gas exit of described reactor is provided with tail gas condenser, described tail gas condenser is communicated with absorption tower, described absorption tower and described absorption liquid water cooler form cooling circuit by described absorption liquid recycle pump, described device also comprises gas blower, described gas blower is connected with the inlet pipe outer end of described reactor.
Preferably, described inlet pipe and feed-pipe stretch into one end tube head sealing in reactor, and the tube wall of described tube head is provided with a plurality of apertures.
Preferably, described absorption liquid recycle pump is also connected with and reclaims mouth, and described recovery mouth is provided with recovery valve.
Preferably, described absorption tower is the multistage ripple packing absorption tower of series connection, and described towers at different levels are respectively by described absorption liquid recycle pump and the conducting of described absorption liquid water cooler.
Preferably, described tail gas condenser is shell and tube or lass lining plate heat interchanger, and cooling medium is 0-15 ℃ of icy salt solution.
Preferably, described gas blower is medium-pressure or high pressure centrifugal blower.
Preferably, described absorption liquid water cooler is the shell and tube heat exchanger of resistance to strong acid corrosion, the recirculated cooling water that cooling medium provides for water cooling tower.
Preferably, described inlet pipe and feed-pipe are the tubing of resistance to nitric acid and hcl corrosion.
Compare with traditional oxidizing reaction and device for absorbing tail gas, device described in the utility model has following remarkable advantage:
1, by adopting the icy salt solution in tail gas condenser to lower the temperature, the condensation of gas of reactor gas-phase escaping is back in reactor, fully recycle partial oxygen agent and maintain the stable of the interior well-oxygenated environment of still, from source, fully recycling the oxygenant of overflowing and realize energy-saving and emission-reduction from still.Realize tail gas simultaneously and entered the precooling before absorption tower, be conducive to alleviate pipeline, equipment high temperature corrosion is aging, promoted absorption process normally to carry out.
2, adopt gas blower to substitute the induced draft fan of absorption system end in prior art, make reactor and tail gas absorb whole system and become malleation from negative pressure, effectively reduced the quick loss of sour gas under negative pressure in stills for air blowing, having increased oxygen recycles in the dissolving of liquid phase at solubleness and the tail gas of liquid phase, and effectively suppressed the desorb in tail gas absorption process, the rate of recovery of nitric acid and the concentration (to 30-35%) of recovery nitric acid have been improved, recovery raw material can directly overlap uses oxidizing reaction, and makes the tail gas qualified discharge after processing.
3, reactor is set up to inlet pipe and feed-pipe, wherein, the pipe end of inlet pipe and feed-pipe is closed, the tube wall of pipe end is provided with a plurality of apertures, by a plurality of apertures being set at inlet pipe pipeline section, make air after aperture is uniformly distributed, directly enter liquid phase, realize fast NO to NO
2conversion and recycling, and avoid NO gas directly to escape from gas phase, make well-oxygenated environment more stable, reduced nitric acid unit consumption, improved oxoethanoic acid yield, by a plurality of apertures being set at feed-pipe pipeline section, nitric acid in nitric acid dropping process is more evenly distributed, alleviated the over oxidation of local concentration of nitric acid due to too high, thus reduced oxalic and other side reaction, improved principal product yield and quality product.
4, on absorption tower, set up absorption liquid water cooler, make absorption tower and absorption liquid water cooler form cooling circuit, make water absorb this exothermic process carries out at lower temperature, improved the solubleness of nitric acid and volatile gas, reduce desorb, absorb more fully, promoted the nitric acid rate of recovery and the synchronous raising of reclaiming concentration of nitric acid.
Accompanying drawing explanation
The oxidizing reaction of modified form synthesizing glyoxalic acid and the structural representation of the device that tail gas absorbs that Fig. 1 provides for the utility model embodiment.
Wherein, 1 reactor, 2 gas blowers, 3 tail gas condensers, 4 absorption towers, 5 absorption liquid recycle pumps, 6 absorption liquid water coolers, 7 feed valves, 8 intake valves, 9 inlet pipe, 10 feed-pipes, 11 agitators, 12 chucks, 13 steam valves, 14 cooling water valves, 15 bleeder valves, 16 air outlet valves, 17 recovery valves, 18 cooling valves, 19 first step absorption tower pneumatic outlets.
Embodiment
For making the purpose of this utility model, technical scheme and advantage clearer, below in conjunction with accompanying drawing, the utility model is described in further detail.
The device that the oxidizing reaction of a kind of modified form synthesizing glyoxalic acid described in the utility model embodiment and tail gas absorb is by 5000L glassed steel reaction vessels 1, centrifugal high pressure (3000Pa < H≤15000 Pa) gas blower 2, heat interchanging area 30 ㎡ graphite modified polypropylene shell and tube tail gas condensers 3, the PP material ripple packing absorption tower 4 of six grades of series connection, six 2.2KW absorption liquid circulation plastic-lining centrifugal pumps 5, six heat interchanging area 80 ㎡ graphite modified polypropylene shell and tube absorption liquid water coolers 6, DN40 PP material charging ball valve 7, DN65 PP material air inlet ball valve 8, the inlet pipe 9 that DN65 PP pipe is made, the feed-pipe 10 that DN40 PP pipe is made.
Referring to Fig. 1, in reactor 1, be provided with inlet pipe 9, feed-pipe 10 and agitator 11, the tube head that inlet pipe 9 and feed-pipe 10 stretch in reactor 1 is closed, the tube wall of tube head is provided with a plurality of apertures, by a plurality of apertures being set at inlet pipe pipeline section, make air after aperture is uniformly distributed, directly enter liquid phase, realize fast NO to NO
2conversion and recycling, and avoid NO gas directly to escape from gas phase, and make nitric acid in nitric acid dropping process be more evenly distributed simultaneously, alleviated the over oxidation of local concentration of nitric acid due to too high, reduce the generation of oxalic acid and other side reaction, improved principal product yield and quality product.Inlet pipe 9 is stretched out on the outer end of reactor 1 and is equipped with for regulating the intake valve 8 of air flow quantity, the outer end that feed-pipe 10 stretches out reactor 1 is provided with feed valve 7, concrete, the inlet pipe in the utility model embodiment and feed-pipe are to be made by the tubing of resistance to nitric acid and hcl corrosion.
In Fig. 1, inlet pipe 9 outer ends connect medium-pressure or high pressure centrifugal blower 2, make reactor and tail gas absorb whole system and become malleation from negative pressure, effectively reduced the quick loss of sour gas under negative pressure in reactor, having increased oxygen recycles in the dissolving of liquid phase at solubleness and the tail gas of liquid phase, and effectively suppressed the desorb in tail gas absorption process, and improved the rate of recovery of nitric acid and the concentration (to 30-35%) of recovery nitric acid, make the tail gas qualified discharge after processing.The bottom of reactor 1 is provided with discharge port, discharge port is provided with bleeder valve 15, after having reacted, open bleeder valve 15, oxidation solution flows out the concentration kettle that enters subsequent processing from discharge port, the outer wall of reactor 1 is provided with the chuck 12 that regulates temperature, chuck 12 is provided with tensimeter, steam-in and cooling water outlet, wherein, the position of steam-in is higher than the position of cooling water outlet, the water coolant cooling water outlet lower from position of being convenient to after steam liquefied discharged, on steam-in and cooling water outlet, be respectively equipped with steam valve 13 and cooling water valve 14, by steam regulation valve 13 and cooling water valve 14, control the temperature in chuck 12, make temperature of reaction in reactor 1 in the scope of process stipulation, on reactor 1, be also provided with the common structures such as thermometer and tensimeter.
As shown in Figure 1, the top of reactor 1 is provided with air outlet, air outlet is provided with air outlet valve 16, the inlet mouth of tail gas condenser 3 is communicated with by conduit with the air outlet of reactor 1, after reaction kettle for reaction completes, the tail gas of reactor 1 interior generation enters tail gas condenser 3 by air outlet, comprises H in tail gas
2o, O
2,nO, NO
2in the utility model embodiment, tail gas condenser 3 is shell and tube or lass lining plate heat interchanger, cooling medium is 0-15 ℃ of icy salt solution, the tail gas of reactor 1 interior generation absorbs and forms HNO3 or HNO2 through water vapour, through the icy salt solution cooling in tail gas condenser 3, condensing reflux, to reactor 1, reaches abundant recycling tail gas again, and maintain the stable of reactor 1 interior well-oxygenated environment, directly from source, fully recycle the oxygenant of overflowing and realize energy-saving and emission-reduction from reactor 1.Realize tail gas simultaneously and entered the precooling before absorption tower, be conducive to alleviate pipeline, equipment high temperature corrosion is aging, promoted absorption process normally to carry out.
As shown in Figure 1, the tail gas that part is not reacted in tail gas condenser 3 enters absorption tower 4 by conduit, the outlet at bottom on absorption tower 4 is connected with absorption liquid recycle pump 5, the other end of absorption liquid recycle pump 5 connects respectively the water-in of absorption liquid water cooler 6 and reclaims the recovery mouth of liquid, reclaim on mouth recovery valve 14 is housed, the water outlet of absorption liquid water cooler 6 is communicated with absorption tower 4, closing reclaim valve 14 in the situation that, absorption tower 4, absorption liquid recycle pump 5 and absorption liquid water cooler 6 form cooling circuit, by absorption liquid recycle pump 5, ceaselessly the liquid that completes in absorption tower 4 is sucked to absorption liquid water cooler 6, be back to again in absorption tower 4, make water absorb this exothermic process carries out at lower temperature, improved the solubleness of nitric acid and volatile gas, reduce desorb, absorb more abundant, the nitric acid rate of recovery and the synchronous raising of reclaiming concentration of nitric acid have been promoted, particularly, in the utility model embodiment, absorption liquid water cooler is the shell and tube heat exchanger of resistance to strong acid corrosion, the recirculated cooling water that cooling medium provides for water cooling tower.
Further, in absorption tower 4 in the utility model embodiment, be provided with six grades of absorption towers, the pneumatic outlet 19 on first step absorption tower is connected with the gas feed on absorption tower, the second stage, series connection successively, until the 6th grade of absorption tower pneumatic outlet lift-off discharge, and every first grade absorption tower is connected and forms cooling circuit separately with an absorption liquid recycle pump and an absorption liquid water cooler respectively.The liquid that completes on absorption towers at different levels is collected by corresponding recovery mouth.By adopting six grades of series connection ripple packing absorption towers, can extend tail gas and absorb flow process, make the contained nox adsorption effect of tail gas even more ideal, further improve the nitric acid rate of recovery, and guarantee that waste gas meets environmental protection standard.
The oxidizing reaction of the improved synthesizing glyoxalic acid described in the utility model embodiment and the working method of device for absorbing tail gas:
Start gas blower 2 and absorption liquid recycle pump 5, feeding sequence according to technological process regulation locates to drop into liquid starting material by feed-pipe 7 in reactor 1, start the agitator 11 of reactor 1, open the air outlet valve 16 of reactor 1, reactor 1 is communicated with tail gas condenser 3, regulates feed valve 7 to control flow, slowly add nitric acid to react, steam regulation valve 13 and cooling water valve 14 in reaction process, control reactor 1 interior reaction temperature in the scope of process stipulation.After adding nitric acid, be incubated for some time, question response is complete, and steam off valve 13 and cooling water valve 14 are opened the bleeder valve 15 of reactor 1, by discharge port vacuum, are turned and are expected to subsequent processing concentration kettle.Close the cooling valve 18 of absorption liquid water cooler 6, open recovery valve 17, the absorption tower rare nitric acid of 4 recovery gained is delivered to recovery mouthful with absorption liquid recycle pump 5 and collects, by adding concentrated nitric acid or purified water, be mixed with rare nitric acid that content is qualified, recycled is in oxidizing reaction.
The implementation result of the device that the oxidizing reaction of the modified form synthesizing glyoxalic acid described in the utility model embodiment and tail gas absorb:
The comparison production test-results that the device that the utility model provides and conventional apparatus are carried out shows: in the situation that other processing condition are substantially constant, in oxidation solution, principal product Determination of Glyoxalic is brought up to 27-29% by former 19-23%; Principal product yield is also significantly improved, and by former molar yield (to oxalic dialdehyde) 75%, brings up to 82%; Reclaim the content of nitric acid and bring up to 38.8-40.2% by former 17-20%, substantially can directly apply mechanically to oxidizing reaction; The nitric acid rate of recovery also brings up to 95.5% by former 83%.The comprehensive unit consumption of nitric acid drops to 0.201t/t(in 50% oxoethanoic acid product by former 0.260t/t).In addition, due to the minimizing of side reaction, the content of some impurity in product is reduced.Aspect environmental protection, after purifying treatment tail gas, 97%(percent by volume wherein) above objectionable impurities is recovered utilization, NO in tail gas
xwith the index of HCl total content lower than 190ppm, wherein NO
xcontent is lower than 175ppm, and HCl content is lower than 10ppm, and the tail gas of discharge meets national environmental standard.
The foregoing is only preferred embodiment of the present utility model, not in order to limit the utility model, all within spirit of the present utility model and principle, any modification of doing, be equal to replacement, improvement etc., within all should being included in protection domain of the present utility model.
Claims (8)
1. the device that the oxidizing reaction of a modified form synthesizing glyoxalic acid and tail gas absorb, it is characterized in that, this device comprises: reactor, tail gas condenser, absorption tower, absorption liquid water cooler, absorption liquid recycle pump, described reactor comprises inlet pipe and feed-pipe, the tail gas exit of described reactor is provided with tail gas condenser, described tail gas condenser is communicated with absorption tower, described absorption tower and described absorption liquid water cooler form cooling circuit by described absorption liquid recycle pump, described device also comprises gas blower, described gas blower is connected with the inlet pipe outer end of described reactor.
2. the device that the oxidizing reaction of modified form synthesizing glyoxalic acid according to claim 1 and tail gas absorb, is characterized in that, described inlet pipe and feed-pipe stretch into one end tube head sealing in reactor, and the tube wall of described tube head is provided with a plurality of apertures.
3. the device that the oxidizing reaction of modified form synthesizing glyoxalic acid according to claim 2 and tail gas absorb, is characterized in that, described absorption liquid recycle pump is also connected with and reclaims mouth, and described recovery mouth is provided with recovery valve.
4. the device that the oxidizing reaction of modified form synthesizing glyoxalic acid according to claim 1 and tail gas absorb, it is characterized in that, described absorption tower is the multistage ripple packing absorption tower of series connection, and described towers at different levels are respectively by described absorption liquid recycle pump and the conducting of described absorption liquid water cooler.
5. the device that the oxidizing reaction of modified form synthesizing glyoxalic acid according to claim 1 and tail gas absorb, is characterized in that, described tail gas condenser is shell and tube or lass lining plate heat interchanger, and cooling medium is 0-15 ℃ of icy salt solution.
6. the device that the oxidizing reaction of modified form synthesizing glyoxalic acid according to claim 1 and tail gas absorb, is characterized in that, described gas blower is medium-pressure or high pressure centrifugal blower.
7. the device that the oxidizing reaction of modified form synthesizing glyoxalic acid according to claim 1 and tail gas absorb, is characterized in that, described absorption liquid water cooler is the shell and tube heat exchanger of resistance to strong acid corrosion, the recirculated cooling water that cooling medium provides for water cooling tower.
8. the device that the oxidizing reaction of modified form synthesizing glyoxalic acid according to claim 1 and tail gas absorb, is characterized in that, described inlet pipe and feed-pipe are the tubing of resistance to nitric acid and hcl corrosion.
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|---|---|---|---|
| CN201420118230.3U CN203741248U (en) | 2014-03-17 | 2014-03-17 | Improved oxidation reaction and tail gas adsorption device for synthesizing glyoxylic acid |
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|---|---|---|---|
| CN201420118230.3U CN203741248U (en) | 2014-03-17 | 2014-03-17 | Improved oxidation reaction and tail gas adsorption device for synthesizing glyoxylic acid |
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| CN104587939A (en) * | 2015-01-07 | 2015-05-06 | 安徽亚格盛电子新材料有限公司 | Device for directly preparing gallium trichloride-tetrahydrofuran solution at normal temperature |
| CN106166470A (en) * | 2016-07-23 | 2016-11-30 | 河南新天地药业股份有限公司 | A kind of dynamic hydraulic combined reaction unit |
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| CN111943287A (en) * | 2020-08-07 | 2020-11-17 | 黑龙江省科学院石油化学研究院 | Ozone circulation reaction system for palladium recovery and palladium recovery method |
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2014
- 2014-03-17 CN CN201420118230.3U patent/CN203741248U/en not_active Expired - Lifetime
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| CN104193772A (en) * | 2014-09-05 | 2014-12-10 | 安徽亚格盛电子新材料有限公司 | Device for de-etherizing trialkyl indium-etherate complex |
| CN104193772B (en) * | 2014-09-05 | 2018-01-02 | 安徽亚格盛电子新材料有限公司 | A kind of trialkyl indium etherate takes off ether device |
| CN104587939A (en) * | 2015-01-07 | 2015-05-06 | 安徽亚格盛电子新材料有限公司 | Device for directly preparing gallium trichloride-tetrahydrofuran solution at normal temperature |
| CN106166470A (en) * | 2016-07-23 | 2016-11-30 | 河南新天地药业股份有限公司 | A kind of dynamic hydraulic combined reaction unit |
| CN106179150A (en) * | 2016-07-23 | 2016-12-07 | 河南新天地药业股份有限公司 | A kind of association response device of Biformyl oxidation synthesis glyoxylate |
| CN107159082A (en) * | 2017-07-08 | 2017-09-15 | 江苏扬子江天悦新材料有限公司 | A kind of specific drugs intermediate reaction bed |
| CN111943287A (en) * | 2020-08-07 | 2020-11-17 | 黑龙江省科学院石油化学研究院 | Ozone circulation reaction system for palladium recovery and palladium recovery method |
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Address after: 438600 Fengshan City, Huanggang province Luotian County, north of the town of water Yi Road, No. 428 Patentee after: HUBEI HONGYUAN PHARMACEUTICAL TECHNOLOGY Co.,Ltd. Address before: 438600 Fengshan City, Huanggang province Luotian County, north of the town of water Yi Road, No. 428 Patentee before: HUBEI HONGYUAN PHARMACEUTICAL Co.,Ltd. |
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Granted publication date: 20140730 |