CN218145875U - Production device for preparing chlorine by byproduct hydrogen chloride - Google Patents
Production device for preparing chlorine by byproduct hydrogen chloride Download PDFInfo
- Publication number
- CN218145875U CN218145875U CN202222800725.1U CN202222800725U CN218145875U CN 218145875 U CN218145875 U CN 218145875U CN 202222800725 U CN202222800725 U CN 202222800725U CN 218145875 U CN218145875 U CN 218145875U
- Authority
- CN
- China
- Prior art keywords
- outlet
- inlet
- tower
- hydrogen chloride
- chlorine
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
A production device for preparing chlorine from byproduct hydrogen chloride comprises a first fan, an organic impurity removal unit, a preheater, a tubular fixed bed reactor, a first condenser, a second absorption tower and a rectification and desorption tower; the first fan is connected with the inlet of the organic impurity removing unit, the outlet of the organic impurity removing unit is connected with the first inlet of the preheater through the gas mixer, the first outlet of the preheater is connected with the inlet of the tubular fixed bed reactor, the outlet of the tubular fixed bed reactor is connected with the second inlet of the preheater, the second outlet of the preheater is connected with the inlet of the first condenser, and the gas outlet of the first condenser is connected with the rectification and desorption tower through the second absorption tower. The utility model is suitable for a chlorine hydride gas that chlorine discarded object released in the pyrolytic treatment process among the direct byproduct hydrogen chloride gas of organic chlorination enterprise's device, external dilute hydrochloric acid and the environmental protection trade etc. is a feasible hydrogen chloride system chlorine's industrial production application technology.
Description
Technical Field
The utility model belongs to the technical field of wade chlorine trade in the processing of byproduct hydrogen chloride utilize, concretely relates to apparatus for producing of chlorine is made to byproduct hydrogen chloride.
Background
Chlorine is an important raw material in various chlorine-related industries, is widely applied to the industries such as chemistry, metallurgy, papermaking, spinning, medicine, pesticide, petrochemical industry, environmental protection and the like, and according to statistics, about one quarter of chemical workers are engaged in production and technical work related to chlorine. More than 200 chlorine-related products exist in China, more than 70 main varieties exist, and the chlorine-related products are mainly used for organically synthesizing PVC, polyurethane intermediates (MDI, TDI, HDI and the like), epoxy resin, organosilicon materials, synthetic rubber, chlorofluorocarbon, synthetic fiber and TiO 2 Chlorine-consuming products such as paints, fuels, organochlorine intermediates (chlorobenzene chloride, chloroacetic acid, benzyl chloride, chlorotoluene, etc.), agricultural and daily chemicals (pesticides, bleaches, disinfectants), building materials, and pharmaceutical preparations. Chinese characterThe production capacity of the required organic chlorine products is the first worldwide, the organic chlorination technology is rapidly developed, the chlorine consumption is extremely high every year, the chlorine is prepared on a large scale mainly by adopting a method for electrolyzing sodium chloride, the energy consumption is high, caustic soda is generated at the same time, and the problem of unbalance between the market demand of the chlorine and the market demand of the caustic soda exists. At present, the market is short of chlorine, and the utilization rate of chlorine atoms is very low in the production process of most chlorine-consuming products. In most organic chlorination reactions, one chlorine atom replaces one hydrogen atom, and the other chlorine atom is combined with the hydrogen atom to generate a hydrogen chloride coproduct (byproduct), so that the utilization rate of the chlorine atom is not more than 50% at most, and the other half of the chlorine atoms are converted into a large amount of byproduct hydrogen chloride; in the production process of polyurethane intermediates such as MDI, TDI and other products, chlorine atoms are only carriers in the phosgenation reaction process and do not enter target products, and 100 percent of chlorine atoms are finally converted into hydrogen chloride; hydrogen chloride is a by-product of chemical reactions involving a large amount of chlorine or phosgene. Along with the rapid increase of the domestic chlorine product productivity, the consumption of chlorine is further increased, and the amount of byproduct hydrogen chloride is also rapidly increased. The byproduct hydrogen chloride has strong corrosivity, high transportation cost, strong market regionality, low price and small demand, and the supply and demand are over, and the alkali neutralization discharge of the excess byproduct hydrogen chloride can cause environmental pollution. The development of a process technology which is environment-friendly, energy-saving and can fully utilize byproduct hydrogen chloride resources is urgently needed.
The byproduct hydrogen chloride generated in the chlorine industry is usually absorbed by water to prepare cheap hydrochloric acid (the byproduct hydrochloric acid usually contains a small amount of organic impurities and limits the application range of the byproduct hydrochloric acid) or is neutralized by alkali and then discharged, so that the economic benefit of the chlorine industry is influenced, and serious environmental pollution is caused. Taking a special essence and special new chemical industry park in a new Lanzhou district as an example, 2000 tons of pymetrozine and byproducts are produced annually by Xinlong Tai Biotech Limited company in Lanzhou, and pymetrozine, chloronicotinic acid and dichloropyrimidine are mainly produced and are high-quality demonstration projects in a green chemical industry park, and the production process needs to be carried outTo use COCl 2 Phosgene, used for preparing pesticide and medicine intermediate isocyanate. Not only Xinlong Tai, but also about 50 projects such as Lanzhou Kangpengwei chemical industry Co., ltd, lanzhou Xinlong Tai Biotech Co., ltd, lanzhou Ruipu Tech Co., ltd, and the like relate to novel pesticide, medicine and veterinary medicine intermediates. The storage, treatment and effective utilization of a large amount of byproduct hydrogen chloride of the enterprises in the garden are urgent problems to be solved by the enterprises. If the generated byproduct hydrogen chloride can be further converted into chlorine, the closed cycle utilization of chlorine elements in a chlorine-related industrial system and the zero emission of a reaction process are realized, the problems of storage, pollution and utilization caused by a large excess of hydrogen chloride can be solved, the continuously increased chlorine demand in the production process of the chlorine industry can be met to a certain extent, the optimization and upgrade of the chlorine-related industry can be promoted, the technology can convert the chlorine-related industry byproduct hydrogen chloride into chlorine, has huge application potential, can bring huge economic benefits, and meets the overall requirements of the modern resource cycle type social development.
The main methods for preparing chlorine gas from hydrogen chloride include an electrolytic method, a direct oxidation method and a catalytic oxidation method. The electrolysis methods include wet methods (membrane point decomposition, oxygen cathode electrolysis) and dry methods, and are very energy-consuming, high in investment cost, and sensitive to impurities contained in hydrogen chloride. The direct oxidation process being by means of NO 2 、SO 3 、HNO 3 、H 2 SO 4 Inorganic oxidants are used for directly oxidizing hydrogen chloride to prepare chlorine, the reaction is carried out in a liquid phase, equipment is complex, corrosive substances are generated in the reaction process, special materials are needed for a reactor, the investment is high, the problems of complex reaction steps, incomplete conversion of hydrogen chloride, a large number of byproducts, low yield, difficult product separation, difficult treatment and discharge of waste gas, difficult waste liquid treatment and the like exist, and the industrialization is difficult to realize. The catalytic oxidation method is a method of oxidizing hydrogen chloride with oxygen or air as an oxidizing agent to produce chlorine gas under the action of a catalyst. Its stoichiometric formula can be represented as:
the catalytic oxidation method is a reversible process of heat release, is proposed for the first time by the 1868 English people Deacon, and at that time, basically all the chlorine produced is obtained by electrolyzing sodium chloride aqueous solution, and the Deacon method does not obtain great attraction; based on the fact that the demand for chlorine is stronger than the demand for sodium hydroxide worldwide, and the condition that a large amount of excessive caustic soda is in short supply of chlorine generally exists in the world, the Deacon method only produces chlorine without producing caustic soda, can well adjust the balance between the market demand of the chlorine and the market demand of the caustic soda, can convert a large amount of low-cost low-value intractable byproduct hydrogen chloride related to the alkali industry into hydrogen chloride with high added value on site, realizes the closed cycle of chlorine and the zero emission of a reaction process, has the advantages of low energy consumption, low equipment cost, simple operation and the like, has huge economic and social benefits, and is the method which has the most prospect and industrialization potential at present.
Chinese patent No. 98812166.2 discloses a method for preparing chlorine by electrolyzing hydrogen chloride by electrochemical method, in the gas-phase electrolysis, the conversion rate of hydrogen chloride is 40% -90%, and unconverted hydrogen chloride is absorbed by lean hydrochloric acid of 5wt% -19wt% to generate rich hydrochloric acid of 6wt% -20wt%, thereby separating chlorine gas from hydrogen chloride gas. The method has the advantages of low hydrogen chloride conversion rate, large electrolysis energy consumption, low concentration of rich hydrochloric acid after absorption of the lean hydrochloric acid, and no overcoming of an azeotrope (azeotropic liquid with the mass fraction of about 20 wt%) of the dilute hydrochloric acid formed by the hydrogen chloride and water, so that the hydrogen chloride gas with higher purity cannot be analyzed.
Chinese patent 200780018069.5 discloses a process for preparing chlorine by catalytic oxidation of hydrogen chloride, then absorbing the hydrogen chloride which is not converted in the product with water to produce hydrochloric acid, and then using electrochemical method to produce chlorine again. This process also does not give a viable hydrogen chloride conversion process.
The existing technologies for preparing chlorine by comprehensively utilizing hydrogen chloride reported in the prior art include an electrochemical method, a method combining catalytic oxidation and electrochemistry, catalytic oxidation in a fluidized bed reactor, purification pretreatment before reaction of hydrogen chloride by ozone or hydrogen peroxide oxidation under ultrasonic wave conditions, a method for preparing chlorine by adopting plasma to realize hydrogen chloride oxidation in a fluidized bed, and the like.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a production device for preparing chlorine by hydrogen chloride byproduct, which has the advantages of reliable production process, simple operation and large operation elasticity.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a production device for preparing chlorine by byproduct hydrogen chloride comprises a raw material pretreatment unit, a catalytic oxidation unit and a product separation and purification unit;
the raw material pretreatment unit comprises a first fan and an organic impurity removal unit;
the catalytic oxidation unit comprises a gas mixer, a preheater, a second heat exchanger and a tubular fixed bed reactor;
the product separation and purification unit comprises a first condenser, a second absorption tower and a rectification and desorption tower;
the first fan is connected with the organic impurity removal unit inlet, the organic impurity removal unit outlet is connected with the gas mixer inlet, the gas mixer outlet is connected with the first inlet of the preheater, the first outlet of the preheater is connected with the inlet of the tubular fixed bed reactor through the second heat exchanger, the outlet of the tubular fixed bed reactor is connected with the second inlet of the preheater, the second outlet of the preheater is connected with the first condenser inlet, the gas outlet of the first condenser is connected with the second absorption tower inlet, and the second absorption tower outlet is connected with the rectification analysis tower.
Further, the organic impurity removal unit comprises a first adsorption tower, a first absorption tower, a concentrated hydrochloric acid buffer tank, a first heat exchanger, a stripping and resolving tower, an absorbent circulating pump, a delivery pump, a concentration tower and a dryer; the outlet of the first fan is divided into two paths, one path is connected with the inlet of the first adsorption tower, and the outlet of the first adsorption tower is connected with the inlet of the dryer; the other path of the outlet of the first fan is connected with the inlet of a first absorption tower, the outlet of the first absorption tower is connected with the inlet of a stripping desorption tower, and the outlet at the top of the stripping desorption tower is connected with the inlet of a dryer; the outlet of the dryer is connected to the inlet of the gas mixer.
Further, the organic impurity removal unit further comprises a second adsorption tower, an inlet of the second adsorption tower is connected with an outlet of the first fan, and an outlet of the second adsorption tower is connected with an inlet of the dryer.
Furthermore, the organic impurity removal unit further comprises a concentrated hydrochloric acid buffer tank and a first heat exchanger, an inlet of the concentrated hydrochloric acid buffer tank is connected with an outlet of the first absorption tower, an outlet of the concentrated hydrochloric acid buffer tank is connected with a first inlet of the first heat exchanger, and a first outlet of the first heat exchanger is connected with an inlet of the stripping analytic tower.
Furthermore, the organic impurity removal unit further comprises a first dilute hydrochloric acid storage tank, an outlet at the bottom of the stripping desorption tower is connected with an inlet of an absorbent circulating pump, an outlet of the absorbent circulating pump is connected with a second inlet of the first heat exchanger, a second outlet of the first heat exchanger is connected with an inlet of the first dilute hydrochloric acid storage tank, and an outlet of the first dilute hydrochloric acid storage tank is connected with the first absorption tower.
Further, a gas distributor is arranged at an inlet at the top of the tubular fixed bed reactor.
Furthermore, a plurality of temperature detectors are arranged in the tube array type fixed bed reactor.
Further, the product separation and purification unit also comprises an absorbent storage tank, a solvent circulating pump and a third heat exchanger;
the outlet of the second absorption tower is connected with the first inlet of the third heat exchanger, and the first outlet of the third heat exchanger is connected with the inlet of the rectification and desorption tower;
the bottom outlet of the rectification and desorption tower is connected with the inlet of the solvent circulating pump, the outlet of the solvent circulating pump is connected with the second inlet of the third heat exchanger, the second outlet of the third heat exchanger is connected with the absorbent storage tank, and the absorbent storage tank is connected with the inlet of the second absorption tower.
Furthermore, a pressure pump is arranged at the outlet of the top of the rectification and desorption tower, and the outlet of the pressure pump is connected with a liquid chlorine storage tank.
Further, the outlet of the tubular fixed bed reactor is connected with the second inlet of the preheater through a fourth fan. Compared with the prior art, the beneficial effects of the utility model are that: the utility model discloses the high temperature reaction gas of shell and tube fixed bed reactor export condenses through the condenser, and the dilute hydrochloric acid after the condensation can further react, or as the absorbent of hydrogen chloride gas. The utility model discloses a shell and tube fixed bed reactor can utilize the heat-carrying agent to realize shifting out and utilizing of reaction heat among the fixed bed reactor. The utility model discloses use hydrogen chloride gas or the dilute hydrochloric acid that contains organic impurity as the raw materials, be applicable to the hydrogen chloride gas etc. that chlorine discarded object released in the pyrolysis treatment process among the direct byproduct hydrogen chloride gas of organic chlorination enterprise's device, external dilute hydrochloric acid and the environmental protection trade, be applicable to the by-product hydrogen chloride of various trades and the high added value production of hydrochloric acid utilizes.
Furthermore, the utility model discloses an add calcium chloride as the auxiliary agent in the concentration tower, break the azeotropic state of mass concentration 20% hydrogen chloride and water, can obtain 30wt% -35wt% concentrated hydrochloric acid.
The utility model discloses can use hydrochloric acid or hydrogen chloride gas as the raw materials, adopt catalytic oxidation technology to produce chlorine, can realize the high added value utilization of by-product hydrogen chloride, the closed cycle of chlorine atom and the zero release of reaction process. The utility model discloses the process is reliable, easy and simple to handle, and operation elasticity is big, is the industrial production application process of feasible hydrogen chloride system chlorine, and it is big to solve the energy consumption that prior art exists, and equipment is complicated, the operation degree of difficulty is big, the gaseous backmixing of fluidized bed, the granule wearing and tearing of catalyst, working costs height, can not big flux or serialization use, be not suitable for the problem that extensive continuous industrialization was used.
Drawings
Fig. 1 is a schematic view of the structure of the device of the present invention.
In the figure, 1, hydrogen chloride gas containing organic impurities; 2. a first fan; 3. a first adsorption column; 4. a second adsorption column; 5. a first stage absorption tower; 6. a first dilute hydrochloric acid storage tank; 7. a concentrated hydrochloric acid buffer tank; 8. a first heat exchanger; 9. stripping and resolving tower; 10. an absorbent circulating pump; 11. an auxiliary agent; 12. an external hydrochloric acid storage tank; 13. a delivery pump; 14. a concentration tower; 15. a dryer; 16. a second fan; 17. a first flow meter; 18. oxygen gas; 19. a third fan; 20. a second flow meter; 21. a gas mixer; 22. a compressor; 23. a pressure reducing valve; 24. a preheater; 25. a second heat exchanger; 26. a tubular fixed bed reactor; 27. a gas distributor; 28. first temperature control; 29. controlling the second temperature; 30. controlling the temperature; 31. a cooling heat carrier; 32. a heat carrier; 33. a fourth fan; 34. a first condenser; 35. a second condenser; 36. a second dilute hydrochloric acid storage tank; 37. a second absorption tower; 38. an absorbent storage tank; 39. a rectification and desorption tower; 40. a solvent circulation pump; 41. a third heat exchanger; 42. a pressure pump; 43. and (4) a liquid chlorine storage tank.
Detailed Description
The following detailed description of the embodiments of the present invention will be made with reference to the accompanying drawings. It is to be understood that the description of the embodiments herein is for purposes of illustration and explanation only and is not intended to limit the invention.
Referring to fig. 1, a production apparatus for producing chlorine gas from hydrogen chloride as a byproduct includes a raw material pretreatment unit, a catalytic oxidation unit, and a product separation and purification unit;
the raw material pretreatment unit comprises a first fan 2, a first adsorption tower 3, a second adsorption tower 4, a first absorption tower 5, a first dilute hydrochloric acid storage tank 6, a concentrated hydrochloric acid buffer tank 7, a first heat exchanger 8, a stripping desorption tower 9, an absorbent circulating pump 10, a delivery pump 13, a concentration tower 14 and a dryer 15; the outlet of the first fan 2 is divided into two paths, one path is connected with the inlets of the first adsorption tower 3 and the second adsorption tower 4, and the outlets of the first adsorption tower 3 and the second adsorption tower 4 are connected with the inlet of the dryer 15. Another way of 2 exports of first fan links to each other with 5 entrances of first absorption tower, 5 exports of first absorption tower link to each other with the entry of concentrated hydrochloric acid buffer tank 7, the export of concentrated hydrochloric acid buffer tank 7 links to each other with the first entry of first heat exchanger 8, the first export of first heat exchanger 8 links to each other with the entry of stripping analytic tower 9, the top export of stripping analytic tower 9 links to each other with the entry of desicator 15, the bottom export of stripping analytic tower 9 links to each other with the entry of absorbent circulating pump 10, the export of absorbent circulating pump 10 links to each other with the second entry of first heat exchanger 8, the second export of first heat exchanger 8 links to each other with the entry of first dilute hydrochloric acid storage tank 6, the export of first dilute hydrochloric acid storage tank 6 links to each other with first absorption tower 5.
The catalytic oxidation unit comprises a second fan 16, a third fan 19, a gas mixer 21, a compressor 22, a pressure reducing valve 23, a preheater 24, a second heat exchanger 25, a tubular fixed bed reactor 26, a gas distributor 27, a first temperature controller 28, a second temperature controller 29 and a third temperature controller 30; wherein, a gas distributor 27 is arranged at the inlet of the top of the tubular fixed bed reactor 26, and a circulating gas distributor is preferably adopted as the gas distributor 27. The outlet of the dryer 15 is connected with a second fan 16, the second fan 16 is connected with the inlet of the gas mixer 21 through a pipeline, and a first flowmeter 17 is arranged on the pipeline; the third fan 19 is connected with the inlet of the gas mixer 21 through a pipeline, and a second flowmeter 20 is arranged on the pipeline; the outlet of the gas mixer 21 is connected to the inlet of a compressor 22, and the outlet of the compressor 22 is connected to a first inlet of a preheater 24 via a pressure reducing valve 23. A first outlet of the preheater 24 is connected to a first inlet of a second heat exchanger 25, and a first outlet of the second heat exchanger 25 is connected to a gas distributor 27. The tubular fixed bed reactor 26 is filled with a cooling heat carrier 31, absorbs heat and then flows out of a hot heat carrier 32.
The product separation and purification unit comprises a fourth fan 33, a first condenser 34, a second condenser 35, a second dilute hydrochloric acid storage tank 36, a second absorption tower 37, an absorbent storage tank 38, a rectification and desorption tower 39, a solvent circulating pump 40, a third heat exchanger 41, a booster pump 42 and a liquid chlorine storage tank 43; wherein, the inlet of the fourth fan 33 is connected with the gas outlet at the bottom of the tubular fixed bed reactor 26, the outlet of the fourth fan 33 is connected with the second inlet of the preheater 24, the second outlet of the preheater 24 is connected with the inlet of the first condenser 34, the first outlet of the first condenser 34 is connected with the inlet of the second condenser 35, and the second outlet of the first condenser 34 and the second outlet of the second condenser 35 are both connected with the second dilute hydrochloric acid storage tank 36; a first outlet of the second condenser 35 is connected with an inlet of the second absorption tower 37, an outlet of the second absorption tower 37 is connected with a first inlet of a third heat exchanger 41, a first outlet of the third heat exchanger 41 is connected with an inlet of a rectification desorption tower 39, a top outlet of the rectification desorption tower 39 is connected with an inlet of a booster pump 42, and an outlet of the booster pump 42 is connected with a liquid chlorine storage tank 43; the bottom outlet of the rectification and desorption tower 39 is connected with the inlet of a solvent circulating pump 40, the outlet of the solvent circulating pump 40 is connected with the second inlet of a third heat exchanger 41, the second outlet of the third heat exchanger 41 is connected with an absorbent storage tank 38, and the absorbent storage tank 38 is connected with the second absorption tower 37.
Removing organic impurities from hydrogen chloride gas containing the organic impurities by adopting a multi-tower parallel switching adsorption method; or aiming at the hydrogen chloride gas containing organic impurities, dilute hydrochloric acid is adopted to circularly absorb the hydrogen chloride gas to produce concentrated hydrochloric acid.
The adsorbent in the first adsorption tower 3 and the second adsorption tower 4 which are operated in parallel is preferably activated carbon or carbon fiber, and the adsorbent is regenerated by steam desorption. The unabsorbed organic impurities can be incinerated to produce steam as a byproduct.
The first dilute hydrochloric acid storage tank 6 is filled with dilute hydrochloric acid, the mass concentration of the dilute hydrochloric acid is 5wt% -20wt%, the concentrated hydrochloric acid buffer tank 7 is filled with concentrated hydrochloric acid, and the mass concentration of the concentrated hydrochloric acid is more than 20wt% and less than or equal to 35wt%.
The dilute hydrochloric acid after passing through the stripping and resolving tower 9 is returned to the first dilute hydrochloric acid storage tank 6 again through the absorbent circulating pump 10 and the first heat exchanger 8, so that waste heat utilization and solvent recycling are realized. In order to break the azeotropic state of the hydrogen chloride and the water with the mass concentration of about 20 percent, a method of adding the auxiliary agent 11 into the concentration tower 14 is adopted as a boiling breaker, so that concentrated hydrochloric acid with the mass concentration of 30 to 35 percent can be obtained. The assistant 11 is calcium chloride with the purity of more than 99.9 percent.
The hydrogen chloride gas is further dried by a dryer 15 to remove trace water and then is sent to a catalytic oxidation unit; the drying agent in the dryer 15 is concentrated sulfuric acid (mass concentration is 98%), zeolite or anhydrous calcium chloride, and concentrated sulfuric acid is preferred. When concentrated sulfuric acid is adopted for drying, the concentrated sulfuric acid absorbs water and becomes dilute sulfuric acid, and the recycling of the sulfuric acid can be realized by adopting vacuum circulating flash evaporation concentration.
The reaction raw material gas is hydrogen chloride and air or hydrogen chloride and oxygen 18, preferably hydrogen chloride and oxygen 18.
In order to mix the reaction raw material gas, namely hydrogen chloride and air or hydrogen chloride and oxygen, a gas mixer 21 is arranged, and the mixed gas regulates and controls the reaction pressure through a compressor 22 and a pressure reducing valve 23.
A plurality of temperature detectors are arranged at different positions in the tubular fixed bed reactor 26, and a plurality of sections of catalysts are arranged in the tubular fixed bed reactor, wherein the upper section of catalyst can further remove organic impurities, and mainly plays a role in protecting the lower section of catalyst; the reaction heat in the tubular fixed bed reactor 26 is removed by the hot carrier 32, so that the waste heat utilization is realized. The heat carrier 32 is preferably molten salt or water, and the heat carried out by the heat carrier 32 can be used as a byproduct of steam. A cold heat carrier 31 is introduced into the tubular fixed bed reactor 26, and flows out of a hot heat carrier 32 after absorbing heat, wherein the hot heat carrier 32 is molten salt, water or heat conducting oil.
The high-temperature reaction gas at the outlet of the tubular fixed bed reactor 26 is cooled and preheated to the feed gas by the preheater 24.
The high-temperature reaction gas is condensed by a first condenser 34 and a second condenser 35 which are connected in series in a multi-stage manner, and the condensed dilute hydrochloric acid can be returned to the raw material external hydrochloric acid storage tank 12 for further reaction or returned to the first dilute hydrochloric acid storage tank 6 in the dilute hydrochloric acid absorption process to be used as an absorbent of hydrogen chloride gas.
The uncondensed gas product enters a second absorption tower 37 for separation, and chlorine in the gas product is absorbed by an absorbent; the absorbent is preferably carbon tetrachloride. The chlorine-containing gas rich solution after chlorine absorption is separated out chlorine gas by a rectification and separation tower 39, and the chlorine gas is compressed by a booster pump 42 and then enters a liquid chlorine storage tank 43; the booster pump 42 is preferably a nano-grade pump.
The barren solution after being resolved by the rectification resolving tower 39 returns to the absorbent storage tank 38 again through the solvent circulating pump 40 and the third heat exchanger 41, so that waste heat utilization and solvent recycling are realized.
But the organic impurity incineration treatment by-product steam of desorption in first adsorption tower 5, steam can be used to the desorption regeneration of adsorbent in first adsorption tower 3 and the second adsorption tower 4.
The unabsorbed oxygen or nitrogen gas in the first absorption tower 5 is directly evacuated. The second absorption tower 37 is directly evacuated without absorbing oxygen or nitrogen. The utility model discloses in can realize absorbing the waste heat utilization and the solvent circulation use of analytic in-process through heat exchanger and circulating pump.
Referring to fig. 1, the working process of the present invention is: the hydrogen chloride gas 1 containing organic impurities, which is a direct byproduct of the device, passes through a first fan 2 and then is treated by switching a first adsorption tower 3 and a second adsorption tower 4 in parallel; or organic impurities in the hydrogen chloride 1 containing the organic impurities are removed through a first absorption tower 5 and a stripping desorption tower 9, and a first dilute hydrochloric acid storage tank 6, a concentrated hydrochloric acid buffer tank 7, a first heat exchanger 8 and an absorbent circulating pump 10 are arranged between the first absorption tower 5 and the stripping desorption tower 9; the hydrogen chloride gas after organic impurities are removed by the second adsorption tower 4 or the stripping and resolving tower 9 further passes through a dryer 15, air or oxygen 18 enters a gas mixer 21 through a third fan 19 and a second flow meter 20, the hydrogen chloride gas enters the gas mixer 21 through a second fan 16 and a first flow meter 17, the air and the hydrogen chloride gas or the oxygen and the hydrogen chloride gas are mixed in the gas mixer 21 according to a certain proportion and then enter a tubular fixed bed reactor 26 through a preheater 24 and a second heat exchanger 25 through a compressor 22 and a pressure reducing valve 23; a gas distributor 27, a first temperature controller 28, a second temperature controller 29 and a third temperature controller 30 are arranged in the tubular fixed bed reactor 26, and heat released by reaction in the tubular fixed bed reactor 26 is removed and utilized through a cold heat carrier 31 and a hot heat carrier 32; the reacted gas product is sent into a preheater 24 through a fourth fan 33 to realize waste heat utilization, dilute hydrochloric acid obtained by condensation of a first condenser 34 and a second condenser 35 which are connected in series enters a second dilute hydrochloric acid storage tank 36, and dilute hydrochloric acid in the second dilute hydrochloric acid storage tank 36 can return to a raw material external hydrochloric acid storage tank 12 or a second dilute hydrochloric acid storage tank 6 in the dilute hydrochloric acid absorption process; the uncondensed gas product enters a second absorption tower 37 for adsorption, the absorbed rich solution passes through a third heat exchanger 41 and then enters a rectification desorption tower 39 for desorption, and the desorbed barren solution enters the third heat exchanger 41 through a solvent circulating pump 40 for heat exchange and then flows back to an absorbent storage tank 38; chlorine gas from the top of the rectification and desorption tower 39 enters a liquid chlorine storage tank 43 after being compressed by a booster pump 42.
The organic impurities removed in the first absorption tower 5 are incinerated to produce steam as a byproduct, and the steam is used for desorption and regeneration of the adsorbents in the first absorption tower 3 and the second absorption tower 4.
The utility model provides two treatment schemes for the direct byproduct of hydrogen chloride containing organic impurities in the device in the chlorine industry in the raw material pretreatment unit, firstly, aiming at the hydrogen chloride gas containing organic impurities, a plurality of adsorption towers are adopted to be connected in parallel to switch to adsorb and remove the organic impurities, and the adsorbent is regenerated by adopting steam desorption; secondly, aiming at the hydrogen chloride gas containing organic impurities, a dilute hydrochloric acid circulating absorption tower and a stripping analysis tower are adopted to remove the organic impurities, and the dilute hydrochloric acid absorbent is recycled and realizes waste heat utilization through a heat exchanger; aiming at the raw material of exotic dilute hydrochloric acid, the azeotropic state of 20 percent of hydrogen chloride and water is broken by adopting a method of adding an auxiliary agent, concentrated hydrochloric acid with the concentration of 30 to 35 percent is obtained by a concentration tower, then the concentrated hydrochloric acid is analyzed out of hydrogen chloride gas by a stripping analysis tower, and the hydrogen chloride is further dried to remove trace water and then enters a catalytic oxidation unit. Hydrogen chloride and air/oxygen in a certain proportion in the catalytic oxidation unit enter a gas mixer through a fan, enter a tubular fixed bed reactor through a compressor and a preheater and react, heat emitted in the reaction process is timely removed through a heat-carrying agent and can be used for byproduct steam, and high-temperature tail gas after the reaction further preheats the feed gas through a heat exchanger. Unconverted hydrogen chloride and product water in the product separation and purification unit are condensed into dilute hydrochloric acid through a multi-stage condenser and returned to a raw material dilute hydrochloric acid storage tank for circulation, trace water in the product is further dried and removed, the target product chlorine is obtained by adopting a solvent absorption and rectification analysis method, the solvent is recycled and the waste heat is utilized in the processes of an absorption tower and a rectification analysis tower, and the chlorine is pressurized by a Nashin pump and then enters a liquid chlorine storage tank. When concentrated sulfuric acid is adopted for drying, the concentrated sulfuric acid absorbs water and becomes dilute sulfuric acid, and the recycling of the sulfuric acid can be realized by adopting vacuum circulating flash evaporation concentration. The utility model is suitable for a chlorine hydride gas etc. that chlorine discarded object released in the pyrolysis treatment process in the direct by-product hydrogen chloride gas of organic chlorination enterprise's device, external dilute hydrochloric acid and the environmental protection trade, the high added value production utilization of by-product hydrogen chloride and hydrochloric acid that is applicable to various trades is the industrial production application technology of a feasible hydrogen chloride system chlorine.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention should be covered by the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (10)
1. A production device for preparing chlorine gas by byproduct hydrogen chloride is characterized by comprising a raw material pretreatment unit, a catalytic oxidation unit and a product separation and purification unit;
the raw material pretreatment unit comprises a first fan (2) and an organic impurity removal unit;
the catalytic oxidation unit comprises a gas mixer (21), a preheater (24), a second heat exchanger (25) and a tubular fixed bed reactor (26);
the product separation and purification unit comprises a first condenser (34), a second absorption tower (37) and a rectification and desorption tower (39);
the first fan (2) is connected with an inlet of an organic impurity removing unit, an outlet of the organic impurity removing unit is connected with an inlet of a gas mixer (21), an outlet of the gas mixer (21) is connected with a first inlet of a preheater (24), a first outlet of the preheater (24) is connected with an inlet of a tubular fixed bed reactor (26) through a second heat exchanger (25), an outlet of the tubular fixed bed reactor (26) is connected with a second inlet of the preheater (24), a second outlet of the preheater (24) is connected with an inlet of a first condenser (34), a gas outlet of the first condenser (34) is connected with an inlet of a second absorption tower (37), and an outlet of the second absorption tower (37) is connected with a rectification and desorption tower (39).
2. The apparatus for producing chlorine from byproduct hydrogen chloride according to claim 1, wherein the organic impurity removal unit comprises a first adsorption tower (3), a first absorption tower (5), a concentrated hydrochloric acid buffer tank (7), a first heat exchanger (8), a stripping and resolving tower (9), an absorbent circulating pump (10), a delivery pump (13), a concentration tower (14), and a dryer (15); the outlet of the first fan (2) is divided into two paths, one path is connected with the inlet of the first adsorption tower (3), and the outlet of the first adsorption tower (3) is connected with the inlet of the dryer (15); the other path of the outlet of the first fan (2) is connected with the inlet of a first absorption tower (5), the outlet of the first absorption tower (5) is connected with the inlet of a stripping desorption tower (9), and the outlet at the top of the stripping desorption tower (9) is connected with the inlet of a dryer (15); the outlet of the dryer (15) is connected to the inlet of the gas mixer (21).
3. The apparatus for producing chlorine from byproduct hydrogen chloride according to claim 2, wherein the organic impurity removing unit further comprises a second adsorption tower (4), an inlet of the second adsorption tower (4) is connected to an outlet of the first fan (2), and an outlet of the second adsorption tower (4) is connected to an inlet of the dryer (15).
4. The apparatus for producing chlorine from byproduct hydrogen chloride according to claim 2, wherein the organic impurity removing unit further comprises a concentrated hydrochloric acid buffer tank (7) and a first heat exchanger (8), an inlet of the concentrated hydrochloric acid buffer tank (7) is connected to an outlet of the first absorption tower (5), an outlet of the concentrated hydrochloric acid buffer tank (7) is connected to a first inlet of the first heat exchanger (8), and a first outlet of the first heat exchanger (8) is connected to an inlet of the stripping desorption tower (9).
5. The production apparatus for producing chlorine by-producing hydrogen chloride according to claim 2, wherein the organic impurity removal unit further comprises a first dilute hydrochloric acid storage tank (6), the bottom outlet of the stripping and resolving tower (9) is connected to the inlet of the absorbent circulating pump (10), the outlet of the absorbent circulating pump (10) is connected to the second inlet of the first heat exchanger (8), the second outlet of the first heat exchanger (8) is connected to the inlet of the first dilute hydrochloric acid storage tank (6), and the outlet of the first dilute hydrochloric acid storage tank (6) is connected to the first absorption tower (5).
6. The apparatus for producing chlorine by-production of hydrogen chloride as claimed in claim 1, wherein a gas distributor (27) is provided at an inlet at the top of the tubular fixed-bed reactor (26).
7. The apparatus for producing chlorine by-production of hydrogen chloride as claimed in claim 1, wherein a plurality of temperature detectors are provided in the tubular fixed-bed reactor (26).
8. The apparatus for producing chlorine by-producing hydrogen chloride according to claim 1, wherein the product separation and purification unit further comprises an absorbent storage tank (38), a solvent circulation pump (40), and a third heat exchanger (41);
an outlet of the second absorption tower (37) is connected with a first inlet of a third heat exchanger (41), and a first outlet of the third heat exchanger (41) is connected with an inlet of a rectification and desorption tower (39);
the bottom outlet of the rectification and desorption tower (39) is connected with the inlet of a solvent circulating pump (40), the outlet of the solvent circulating pump (40) is connected with the second inlet of a third heat exchanger (41), the second outlet of the third heat exchanger (41) is connected with an absorbent storage tank (38), and the absorbent storage tank (38) is connected with the inlet of a second absorption tower (37).
9. The apparatus for producing chlorine by-producing hydrogen chloride as claimed in claim 1, wherein a pressure pump (42) is provided at an outlet at the top of the rectification/desorption column (39), and a liquid chlorine storage tank (43) is connected to an outlet of the pressure pump (42).
10. The apparatus for producing chlorine by-production of hydrogen chloride as claimed in claim 1, wherein the outlet of the tubular fixed-bed reactor (26) is connected to the second inlet of the preheater (24) via a fourth fan (33).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222800725.1U CN218145875U (en) | 2022-10-24 | 2022-10-24 | Production device for preparing chlorine by byproduct hydrogen chloride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222800725.1U CN218145875U (en) | 2022-10-24 | 2022-10-24 | Production device for preparing chlorine by byproduct hydrogen chloride |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218145875U true CN218145875U (en) | 2022-12-27 |
Family
ID=84570975
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202222800725.1U Active CN218145875U (en) | 2022-10-24 | 2022-10-24 | Production device for preparing chlorine by byproduct hydrogen chloride |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218145875U (en) |
-
2022
- 2022-10-24 CN CN202222800725.1U patent/CN218145875U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109134231B (en) | Device and process for continuously producing chloroacetic acid by differential circulation | |
| CN104311383B (en) | A kind of method of the hydrogen chloride production monochloro methane that utilizes by-product in tetrachloro-ethylene production process | |
| CN109503312B (en) | Process for continuously producing chloroethane by using byproduct hydrogen chloride produced in chlorobenzene production | |
| KR101952451B1 (en) | Process for the preparation of isocyanates | |
| CN214399818U (en) | Device for purifying hydrogen chloride by calcium chloride method containing impurity dilute hydrochloric acid | |
| CN111330412B (en) | System and process for absorbing and purifying byproduct hydrogen chloride gas in chlorination section into acid | |
| CN113398719A (en) | Device and method for recovering chlorine in tail chlorine | |
| CN100562487C (en) | The complete recovering technique of hydrogenchloride in the industrial gasses | |
| CN102285651A (en) | Purification and recycling method of CO in phosgene synthesis unit tail gas | |
| US20080260619A1 (en) | Processes for the oxidation of hydrogen chloride | |
| CN111285331A (en) | Method for preparing hydrobromic acid and sodium bromide from bromine-containing brine in short process | |
| CN218145875U (en) | Production device for preparing chlorine by byproduct hydrogen chloride | |
| CN205164495U (en) | System for handle gas -solid looks chlorination high polymer tail gas | |
| CN103497085A (en) | Processes for bi-coproduction and tri-coproduction of methyl chloride, methane chloride, and tetrachloroethylene | |
| CN106000075B (en) | The purification absorption of chlorinated exhaust and circulation utilization method and device in benzene chloridization process | |
| CN112028089A (en) | Ammonium nitrate production device and method | |
| CN201101938Y (en) | Completely recycling system for hydrogen chloride in industry gas | |
| CN115571857A (en) | Production process and device for preparing chlorine gas by using byproduct hydrogen chloride | |
| CN212369872U (en) | System for absorbing and purifying byproduct hydrogen chloride gas in chlorination workshop section to form acid | |
| CN115348956A (en) | Process for producing chloroethane | |
| CN214383703U (en) | Low-concentration impurity-containing dilute hydrochloric acid hydrogen chloride purification device by sulfuric acid method | |
| CN205850525U (en) | A kind of for processing the device of tail gas in benzene chloride production | |
| CN110240536A (en) | A kind of production of vinyl chloride and process for refining | |
| CN107973692A (en) | A kind of preparation method of brominated alkanes | |
| CN109651072B (en) | Method for preparing chloroethane from hydrochloric acid containing sulfur dioxide |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |