CN104744209A - Moving-bed reactor for recycling ammonia and hydrogen chloride through ammonium chloride chemical chain circulation and application of moving-bed reactor - Google Patents
Moving-bed reactor for recycling ammonia and hydrogen chloride through ammonium chloride chemical chain circulation and application of moving-bed reactor Download PDFInfo
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Abstract
The invention discloses a moving-bed reactor for recycling ammonia and hydrogen chloride through ammonium chloride chemical chain circulation. The moving-bed reactor comprises a heat-preservation shell, wherein the heat-preservation shell is internally provided with an inner reactor cylinder and a fume channel for providing heat energy to the inner reactor cylinder; a solid feeding hole is formed in one end of the inner reactor cylinder; a gas feeding hole is formed in the other end of the inner reactor cylinder. The moving-bed reactor disclosed by the invention comprises a septate heat transfer type reactor and a heat accumulation type reactor; for the septate heat transfer type reactor, high-temperature fume can provide energy to the chlorine release process through the fume channel; for the heat accumulation type reactor, air is subjected to heat exchange and is heated through a heat accumulator at one end and is mixed and combusted with a fuel gas in a combustion area, so that energy can be provided for the chlorine release process, and the waste heat of the fume is recycled through another heat accumulator at the other end. The invention further discloses a method for recycling hydrogen chloride by using the moving-bed reactor.
Description
Technical field
The present invention relates to chemical production field, be specifically related to a kind of soda ash based on ammonium chloride recycle chemistry chain-vinylchlorid joint process and moving-burden bed reactor.
Background technology
Chemical chain refers to the process completed by the effect point polystep reaction of chemical mediator by a certain specific chemical reaction.This concept just was once used to react with water vapour and iron prepare hydrogen at the beginning of last century, and commercially producing for carbonic acid gas.In recent years, because carbon fuel combustion recycle chemistry chain process can obtain the carbonic acid gas Gong sealing up for safekeeping, the research and development of carbon fuel combustion chemical chain technique is day by day deep.On the other hand, except carbon fuel combustion, other recycle chemistry chain process studies are relatively less.In fact, in traditional chemical industry process, the thinking of recycle chemistry chain is worth extensively using for reference and Application and Development, as the chemical chain problem of chlorine in chlorine industry, and the circulatory problems etc. of ammonia in soda ash technique.
Soda ash and vinylchlorid belong to inorganic chemical industry and organic chemical industry's industry respectively, and both produce generally from founding the factory to be all completely independently, associates less.Both domestic production capacity scales are large, all reach ten-million-ton scale other.At present, domestic soda ash technique all adopts union soda, although union soda solves the waste solution of calcium chloride problem produced in ammonia alkali process, side product sodium chloride product, along with the continuous expansion of soda industry scale, the output of ammonium chloride grows with each passing day.Because ammonium chloride can cause soil acidification as nitrogenous fertilizer, limited as Fertilizer Market, ammonium chloride overstocks the bottleneck having become soda industry development in a large number.
Domestic calcium carbide/acetylene method process for vinyl chloride mainly comprises three parts: 1), with carbon element and calcium oxide for raw material, calcium carbide (carbide of calcium) is generated by electrode heat, calcium oxide is obtained by limestone calcination, and calcium carbide obtains acetylene by hydrolysis again; 2), adopt sodium chloride salt water electrolysis method to generate chlorine, hydrogen and caustic soda, chlorine and hydrogen carry out being obtained by reacting hydrogenchloride again; 3), acetylene and hydrogenchloride carry out hydrochlorination and obtain vinylchlorid on mercuric chleride catalyst.In calcium carbide/acetylene method process for vinyl chloride, often produce 1 ton of calcium oxide, about 0.8 ton of CO need be discharged
2, generate 1.3 ~ 1.8 tons of solid carbide slags simultaneously, all severe contamination caused to environment; Meanwhile, calcium carbide is produced and is adopted high temperature electrode scorification, and hydrogen chloride production adopts saline electrolysis method, all belongs to high energy consumption technique; Due to byproduct caustic soda market, supply exceed demand, also limit the development of process for vinyl chloride.
As from the foregoing, existing soda ash and process for vinyl chloride bring a large amount of wastings of resources and environmental pollution respectively, need badly and improve relevant technologies.Current main thought is that two techniques are carried out integrated optimization, reaches the object of energy-saving and emission-reduction, obtains efficient soda ash-vinylchlorid joint process.We have been a kind of method that patent document discloses soda ash and vinylchlorid combination producing of CN103626206A at publication number, first carrier and ammonium chloride reactive absorption hydrogenchloride is utilized, discharge ammonia, then the carrier of absorbing hydrogen chloride is heated, discharge hydrogenchloride; Then the ammonia obtained and sodium chloride aqueous solution and carbon dioxide reaction are produced soda ash, the ammonium chloride cyclically utilizing of by-product; The hydrogenchloride obtained and acetylene reaction are produced vinylchlorid, and the carbonic acid gas reuse of acetylene preparation process by-product, to soda manufacture, discharges the carrier loop reuse after hydrogenchloride.Ammonium chloride recycle chemistry chain technology of the present invention, integrated existing soda ash and vinylchlorid production technique, solve ammonium chloride circulatory problems, is expected to the low ammonia or the zero ammonia consumption that realize soda ash technique; Simplify soda ash and process for vinyl chloride, significantly reduce fund input and energy consumption.
But how effectively ammonium chloride is prepared by recycle chemistry chain technology the key point that hydrogenchloride and ammonia are integrated techniques, be therefore the prerequisite of existing soda ash-vinylchlorid joint process integrated optimization based on the moving-burden bed reactor technology of recycle chemistry chain.The present invention releases chlorine process for research object with joint process, in early stage under having made the prerequisite of systematic study in the screening and assessment, optimization of process conditions etc. of joint process thermodynamic process, carrier, have extensively studied pyrolysis kinetics and the reactor technology of containing hydrogen chloride carrier, propose the moving-burden bed reactor technology disclosed in this patent.
Summary of the invention
The object of the present invention is to provide a kind of moving-burden bed reactor based on ammonium chloride recycle chemistry chain, and be applied to efficient soda ash-vinylchlorid coproduction technique.
Concrete technical scheme of the present invention is as follows:
Based on an application for the moving-burden bed reactor of ammonium chloride recycle chemistry chain, the following technological process of main generation:
(1) by carrier and ammonium chloride blending transportation to moving-burden bed reactor A, react at a lower temperature and discharge ammonia, then reuse is to soda ash technique unit for the ammonia of acquisition, and the ammonium chloride of by-product continues to be provided to step (1);
(2) again the carrier being adsorbed with hydrogenchloride is delivered to moving-burden bed reactor B, at relatively high temperatures pyrolysis discharge hydrogenchloride, the hydrogenchloride of acquisition is delivered to process for vinyl chloride unit, the carrier after release hydrogenchloride then reuse to step (1);
(3) above-mentioned process energy is provided by flue fuel combustion or high-temperature flue gas sensible heat.
As preferably, in step (1) during decomposing ammonium chloride, ammonium chloride and rare gas element are delivered in moving-burden bed reactor A, at 200 ~ 400 DEG C, and reaction 0.1 ~ 2h in reactor;
As preferably, during hydrogenchloride in step (2) in release vehicle, the carrier being absorbed with hydrogenchloride is delivered in moving-burden bed reactor B, at 500 ~ 700 DEG C, reacts 0.1 ~ 2h; Also the carrier and rare gas element that are absorbed with hydrogenchloride can be delivered to release in chlorine reactor jointly and react.
As preferably, described carrier is the mixture of magnesium oxide and hydroxy chloride magnesium, and wherein the molar content of hydroxy chloride magnesium should be no less than 10%, and after process, the transformation efficiency of hydroxy chloride magnesium is 0.85 ~ 1.
The reaction that moving-burden bed reactor of the present invention relates to mainly comprises " low temperature releases ammonia " and " high temperature releases chlorine " two processes, to release chlorine process, releases in chlorine reactor and reacts as follows:
Mg (OH) Cl → MgO+HCl ↑ (master) (1)
Mg(OH)Cl+HCl↑→MgCl
2+H
2O↑ (2)
Obtain the mixed gas being rich in HCl after reaction, through dedusting, cooling, refining after obtain highly purified hydrogen chloride gas, and deliver to process for vinyl chloride unit, carrier is recycled to and releases ammonia reactor and recycle simultaneously.In obvious ammonium chloride recycle chemistry chain process, it is endothermic process that high temperature releases chlorine process, and therefore the efficient heat supply of relevant reactor is key problem in technology of the present invention.
Reclaim a moving-burden bed reactor for ammonia and hydrogenchloride for ammonium chloride recycle chemistry chain, comprise lagging casing, be provided with reactor inner core in described lagging casing and provide the exhaust gases passes of heat energy for reactor inner core; One end of reactor inner core has feeding-in solid body mouth, and the other end has gas feed mouth.
In order to prevent gaseous product contaminated, release ammonia reactor and release chlorine reactor and all should adopt septate heat transfer, therefore chlorine reactor of releasing of the present invention adopts external-heat moving-bed, in external-heat moving-bed, recycle chemistry chain carrier material and thermal medium are by septate heat transfer, and heat-supplying mode adopts fuel gas buring heat supply or high-temperature flue gas indirect heat exchange.
As preferably, feeding-in solid body mouth and gas discharge port are positioned at same one end of reactor inner core, gas feed mouth and solids exit mouth are positioned at same one end of reactor inner core, namely material and gas in reactor in reversely to pass into, inner core material and gas oppositely pass into and are more conducive to mutual mass transfer and reaction, can suppress the generation of side reaction better.
As preferably, the two ends of exhaust gases passes are respectively equipped with inlet mouth and air outlet; According to partition heat-exchanging moving-bed, pass into high-temperature flue gas in exhaust gases passes, high-temperature flue gas airintake direction can be identical with mass transport direction or contrary; According to thermal storage type moving bed, what inlet mouth passed into is air.
In thermal storage type moving bed, Two-cuff Technique body is arranged at the two ends of described exhaust gases passes, and the flue gas channel part between described Two-cuff Technique body is combustion zone, is provided with burner noz(zle) in described combustion zone; The heat storage of one end is used for carrying out heat exchange intensification to the air passed into, and burns in combustion zone and combustion gas mixing and provide energy for releasing chlorine process, and the flue gas after burning carries out waste heat recovery by the other end heat storage.
Preferably, described air outlet is connected with reversing valve, and a road of reversing valve is for discharging gas, and described inlet mouth is led on another road.In reactor operational process, scope switching time of reversing valve is 100 ~ 1200s, and reversing valve for changing the flow direction of flue gas and air, thus provides condition for the accumulation of heat of heat storage and exothermic process.Switching time is too short, is unfavorable for that heat storage is to preheating of air; And switching time is oversize, be unfavorable for heat storage Mist heat recovering.
Moving-burden bed reactor type of the present invention has two kinds, is respectively partition heat-exchanging moving-bed and thermal storage type moving bed.Partition heat-exchanging moving-burden bed reactor mainly comprises the devices such as reactor inner core, exhaust gases passes, lagging casing.
As preferably, high-temperature flue gas entry temperature range is 900 ~ 1300 DEG C, and in reactor operational process, flue gas exit temperature should be limited in 25 ~ 250 DEG C, to ensure higher heat recuperation rate.
Described thermal storage type moving bed reactor mainly comprises the devices such as reactor inner core, exhaust gases passes, lagging casing, burner noz(zle), heat storage, reversing valve, and wherein heat storage is arranged at exhaust gases passes both sides, and burner noz(zle) is then evenly arranged in combustion zone.
As preferably, for structure of reactor, reaction zone length range is 10 ~ 50m, and heat storage length range is 1 ~ 5m, namely the length of single heat storage accounts for 1/10 ~ 1/2 of reaction zone length, and heat storage length is too short does not meet the requirement that heat storage absorbs fume afterheat; The investment of the oversize increase reactor apparatus of heat storage length thus increase cost of equipment, extends the loss of the residence time build-up of pressure of gas in heat storage simultaneously, can cause the raising of process cost.
The moving-burden bed reactor that the present invention relates to is described as follows:
To release chlorine process, releasing in chlorine moving-burden bed reactor, the carrier (hydroxy chloride magnesium) of rare gas element and absorbing hydrogen chloride is simultaneously respectively at moving-burden bed reactor inner core two ends continus convergence, for partition heat-exchanging, high-temperature flue gas provides energy via exhaust gases passes for releasing chlorine process, and flue gas airintake direction can be identical with mass transport direction or contrary; For heat accumulating type, air to burn in combustion zone and combustion gas mixing after heating up via one end heat storage heat exchange and provides energy for releasing chlorine process, flue gas then by the other end heat storage for recovery waste heat, after switching time, air commutates and repeats said process.Carrier material absorbs heat and reacts in course of conveying, and gaseous mixture is delivered to step (2) after later separation, and after reaction, carrier discharging is then back to use step (1) recycle.
Tool of the present invention has the following advantages:
Process aspect: 1) solve ammonium chloride circulatory problems; By above-mentioned moving-burden bed reactor is applied to soda ash-vinylchlorid joint process, be expected to the low ammonia or the zero ammonia consumption that realize soda ash technique.2) Simplified flowsheet, reduces investment outlay; By above-mentioned moving-burden bed reactor is applied to soda ash-vinylchlorid joint process, can be soda ash technique and save carbonic acid gas manufacture and the purification systems such as limestone kiln, for process for vinyl chloride saves ion film caustic soda and hydrogen chloride synthesis system, significantly reduce investment outlay.3) energy-saving and cost-reducing; By above-mentioned moving-burden bed reactor is applied to soda ash-vinylchlorid joint process, the chloralkali process of electrolytic process HCl can be replaced, significantly reduce power consumption in production process; Save soda ash limestone kiln simultaneously, significantly reduce energy consumption.
Reactor aspect: 1) for partition heat-exchanging moving-burden bed reactor, simplify structure of reactor, effectively reduce facility investment, reduces operation easier.2) for thermal storage type moving bed, be integrated with moving-bed and Regenerative Combustion Technology, fully improve heat utilization ratio.
Accompanying drawing explanation
Fig. 1 is the thermal storage type moving bed reactor sketch based on ammonium chloride recycle chemistry chain of the present invention;
Fig. 2 is the partition heat-exchanging moving-burden bed reactor sketch based on ammonium chloride recycle chemistry chain of the present invention;
Fig. 3 is the side-view of Fig. 2 midfeather heat exchange type moving-burden bed reactor.
Embodiment
As shown in Figure 1, a kind of thermal storage type moving bed reactor based on ammonium chloride recycle chemistry chain, comprises lagging casing 105, reactor inner core 104, exhaust gases passes 102, rotary motion mechanism 103, heat storage 106, burner noz(zle) 107 and reversing valve 108.One end of reactor inner core 104 is used for feeding-in solid body and gas discharge, and the other end is used for solids exit and gas feed, and solid is contrary with transfer of gas direction.The two ends of exhaust gases passes 102 are equipped with heat storage 106, burner noz(zle) 107 is evenly arranged in combustion zone between two heat storages 106, the heat storage 106 of one end is for carrying out heat exchange intensification to the air passed into, and burn in combustion zone and combustion gas mixing and provide energy for releasing chlorine process, flue gas after burning carries out waste heat recovery by the other end heat storage 106, carry out control combustion nozzle 107 gas flow by temperature in detection reaction device simultaneously, ensure continuity and the stability of operating mode.Reversing valve 108 is arranged in the exhaust line of exhaust gases passes 102.
Embodiment 1
Release chlorine process to carry out in the thermal storage type moving bed reactor shown in Fig. 1, reaction mass is the solid-phase material obtained after releasing ammonia process, the i.e. mixture of magnesium oxide (recycle chemistry chain carrier) and hydroxy chloride magnesium, mixture feedstock quality flow is 2.3t/h, average transfer rate is 20m/h, wherein the mol ratio of magnesium oxide and hydroxy chloride magnesium is about 1:2, meanwhile reversely in cylinder in reaction process pass into a certain amount of atmospheric steam, wherein water vapour is provided by the vaporizer of 200 DEG C.Two-cuff Technique body is arranged at moving-burden bed reactor two ends, and be evenly arranged burner noz(zle) in exhaust gases passes, normal temperature lower volume flow is about 1720m
3the air of/h is via the Sweet natural gas mixed firing being about 93kg/h after one end heat storage heat exchange intensification in combustion zone and mass rate, about 1049kW energy is provided for releasing chlorine process, after reaction, high-temperature flue gas is then by the other end heat storage recovery waste heat, reactor length is 10m, single heat storage length is 3m, turnaround time is when being 1250s, the residence time of solid-phase material in moving-burden bed reactor is about 50min, the highest temperature out of final flue gas controls below 250 DEG C, and solid-phase material temperature out is about 670 DEG C, wherein the transformation efficiency of hydroxy chloride magnesium reaches 95%, reactor thermo-efficiency is higher than 85%.After reaction inner core outlet mixed gas through follow-up dedusting, cooling, refining after the high purity hydrogen chloride gas that obtains deliver to the raw material of vinylchloride units as synthesizing chloroethylene, solid phase discharging then cyclically utilizing to ammonium chloride centrifugal station as the chemical chain carrier releasing ammonia react.
As shown in Figures 2 and 3, a kind of partition heat-exchanging moving-burden bed reactor based on ammonium chloride recycle chemistry chain, comprises lagging casing 205, reactor inner core 204, exhaust gases passes 202 and rotary motion mechanism 203.One end of reactor inner core 204 is used for feeding-in solid body and gas discharge, and the other end is used for solids exit and gas feed, and solid is contrary with transfer of gas direction.Pass into high-temperature flue gas in exhaust gases passes 202, provide energy by the mode of septate heat transfer for releasing chlorine process, high-temperature flue gas airintake direction can be identical with mass transport direction or contrary.
Embodiment 2
Release chlorine process to carry out in the partition heat-exchanging moving-burden bed reactor shown in Fig. 2, reaction mass is the solid-phase material obtained after releasing ammonia process, the i.e. mixture of magnesium oxide (recycle chemistry chain carrier) and hydroxy chloride magnesium, mixture feedstock quality flow is 2.3t/h, material inlet temperature is normal temperature, average transfer rate is 20m/h, wherein the mol ratio of magnesium oxide and hydroxy chloride magnesium is about 1:2, meanwhile reversely in cylinder in reaction process pass into a certain amount of atmospheric steam, wherein water vapour is provided by the vaporizer of 200 DEG C.5m is passed in exhaust gases passes
3/ s high-temperature flue gas provides energy for releasing chlorine process, smoke inlet temperature is 1500K, and airintake direction is contrary with mass transport direction, when reactor length is 40m, the residence time of solid-phase material in moving-burden bed reactor is 120min, final solid-phase material temperature out is about 650 DEG C, and wherein the transformation efficiency of hydroxy chloride magnesium reaches 89%, and reactor thermo-efficiency reaches 56%.After reaction inner core outlet mixed gas through follow-up dedusting, cooling, refining after the high purity hydrogen chloride gas that obtains deliver to the raw material of vinylchloride units as synthesizing chloroethylene, solid phase discharging then cyclically utilizing to ammonium chloride centrifugal station as the chemical chain carrier releasing ammonia react.
Embodiment 3
Release chlorine process to carry out in the partition heat-exchanging moving-burden bed reactor shown in Fig. 2, reaction mass is the solid-phase material obtained after releasing ammonia process, the i.e. mixture of magnesium oxide (recycle chemistry chain carrier) and hydroxy chloride magnesium, mixture feedstock quality flow is 2.3t/h, material inlet temperature is normal temperature, average transfer rate is 20m/h, wherein the mol ratio of magnesium oxide and hydroxy chloride magnesium is about 1:2, meanwhile reversely in cylinder in reaction process pass into a certain amount of atmospheric steam, wherein water vapour is provided by the vaporizer of 200 DEG C.10m is passed in exhaust gases passes
3/ s high-temperature flue gas provides energy for releasing chlorine process, smoke inlet temperature is 1300K, and airintake direction is contrary with mass transport direction, when reactor length is 30m, the residence time of solid-phase material in moving-burden bed reactor is 90min, final solid-phase material temperature out is about 638 DEG C, and wherein the transformation efficiency of hydroxy chloride magnesium reaches 87%, and reactor thermo-efficiency is 38%.After reaction inner core outlet mixed gas through follow-up dedusting, cooling, refining after the high purity hydrogen chloride gas that obtains deliver to the raw material of vinylchloride units as synthesizing chloroethylene, solid phase discharging then cyclically utilizing to ammonium chloride centrifugal station as the chemical chain carrier releasing ammonia react.
The preferred counterflow moving bed reactor parameter of table 1
Embodiment 4
Release chlorine process to carry out in the partition heat-exchanging moving-burden bed reactor shown in Fig. 2, reaction mass is the solid-phase material obtained after releasing ammonia process, the i.e. mixture of magnesium oxide (recycle chemistry chain carrier) and hydroxy chloride magnesium, mixture feedstock quality flow is 2.3t/h, material inlet temperature is normal temperature, average transfer rate is 20m/h, wherein the mol ratio of magnesium oxide and hydroxy chloride magnesium is about 1:2, meanwhile reversely in cylinder in reaction process pass into a certain amount of atmospheric steam, wherein water vapour is provided by the vaporizer of 200 DEG C.20m is passed in exhaust gases passes
3/ s high-temperature flue gas provides energy for releasing chlorine process, smoke inlet temperature is 1500K, and airintake direction is identical with mass transport direction, when reactor length is 13m, the residence time of solid-phase material in moving-burden bed reactor is about 40min, final solid-phase material temperature out is about 660 DEG C, and wherein the transformation efficiency of hydroxy chloride magnesium reaches 93.5%, and reactor thermo-efficiency is 32%.After reaction inner core outlet mixed gas through follow-up dedusting, cooling, refining after the high purity hydrogen chloride gas that obtains deliver to the raw material of vinylchloride units as synthesizing chloroethylene, solid phase discharging then cyclically utilizing to ammonium chloride centrifugal station as the chemical chain carrier releasing ammonia react.
Embodiment 5
Release chlorine process to carry out in the partition heat-exchanging moving-burden bed reactor shown in Fig. 2, reaction mass is the solid-phase material obtained after releasing ammonia process, the i.e. mixture of magnesium oxide (recycle chemistry chain carrier) and hydroxy chloride magnesium, mixture feedstock quality flow is 2.3t/h, material inlet temperature is normal temperature, average transfer rate is 20m/h, wherein the mol ratio of magnesium oxide and hydroxy chloride magnesium is about 1:2, meanwhile reversely in cylinder in reaction process pass into a certain amount of atmospheric steam, wherein water vapour is provided by the vaporizer of 200 DEG C.30m is passed in exhaust gases passes
3/ s high-temperature flue gas provides energy for releasing chlorine process, smoke inlet temperature is 1300K, and airintake direction is identical with mass transport direction, when reactor length is 20m, the residence time of solid-phase material in moving-burden bed reactor is 60min, final solid-phase material temperature out is about 655 DEG C, and wherein the transformation efficiency of hydroxy chloride magnesium reaches 92%, and reactor thermo-efficiency is 35%.After reaction inner core outlet mixed gas through follow-up dedusting, cooling, refining after the high purity hydrogen chloride gas that obtains deliver to the raw material of vinylchloride units as synthesizing chloroethylene, solid phase discharging then cyclically utilizing to ammonium chloride centrifugal station as the chemical chain carrier releasing ammonia react.
The preferred cocurrent flow type moving-burden bed reactor parameter of table 2
The parameters optimization of the different moving-burden bed reactor of table 3 compares
As seen from the results in Table 3, based on similar structure of reactor size, the thermal efficiency value of indirect heat exchange type moving-burden bed reactor after optimizing is still well below thermal storage type moving bed.Reason is that the ceramic honey comb heat storage capacity of thermal storage type moving bed employing is strong, and accumulation of heat is fast, can absorb fume afterheat preferably on the one hand, on the other hand high-temperature zone energy is supplied to material reaction, greatly improves capacity usage ratio.
The present invention also may have other implementation method, but no matter which kind of technical scheme, all can not change technical characteristic of the present invention, any moving-burden bed reactor technology based on ammonium chloride recycle chemistry chain technology all belongs to scope of the present invention.
Claims (10)
1. reclaim a moving-burden bed reactor for ammonia and hydrogenchloride for ammonium chloride recycle chemistry chain, comprise lagging casing, it is characterized in that, in described lagging casing, be provided with reactor inner core reaction zone, and provide the exhaust gases passes of heat energy for reactor; The two ends of reactor inner core have solid, gas feed and discharge port; Solid reactant passes through reaction zone in the mode of plug flow.
2. the moving-burden bed reactor of ammonia and hydrogenchloride is reclaimed as claimed in claim 1 for ammonium chloride recycle chemistry chain, it is characterized in that, feeding-in solid body mouth and gas discharge port are positioned at same one end of reactor inner core, and gas feed mouth and solids exit mouth are positioned at same one end of reactor inner core.
3. reclaim the moving-burden bed reactor of ammonia and hydrogenchloride as claimed in claim 1 for ammonium chloride recycle chemistry chain, it is characterized in that, the two ends of exhaust gases passes are respectively equipped with inlet mouth and air outlet.
4. reclaim the moving-burden bed reactor of ammonia and hydrogenchloride as claimed in claim 3 for ammonium chloride recycle chemistry chain, it is characterized in that, Two-cuff Technique body is arranged at the two ends of described exhaust gases passes.
5. reclaim the moving-burden bed reactor of ammonia and hydrogenchloride as claimed in claim 4 for ammonium chloride recycle chemistry chain, it is characterized in that, single heat storage length accounts for 1/10 ~ 1/2 of reaction zone length.
6. reclaim the moving-burden bed reactor of ammonia and hydrogenchloride as claimed in claim 4 for ammonium chloride recycle chemistry chain, it is characterized in that, the flue gas channel part between described Two-cuff Technique body is combustion zone, is provided with burner noz(zle) in described combustion zone.
7. reclaim the moving-burden bed reactor of ammonia and hydrogenchloride as claimed in claim 6 for ammonium chloride recycle chemistry chain, it is characterized in that, described air outlet is connected with reversing valve, and a road of reversing valve is for discharging gas, and described inlet mouth is led on another road.
8. the moving-burden bed reactor according to any one of claim 1 ~ 7 is applied to the method reclaiming hydrogenchloride, it is characterized in that, comprise step: the carrier of rare gas element and absorbing hydrogen chloride is respectively by reactor inner core two ends continus convergence, the chlorine process of releasing that exhaust gases passes is reactor inner core provides energy, the carrier loop that Reaction Separation obtains utilizes, and mixed gas is delivered to process for vinyl chloride unit after later separation.
9. moving-burden bed reactor as claimed in claim 8 is applied to the method reclaiming hydrogenchloride, and it is characterized in that, the high-temperature flue gas entry temperature range of exhaust gases passes is 900 ~ 1300 DEG C, and flue gas exit temperature is limited in 25 ~ 250 DEG C.
10. moving-burden bed reactor as claimed in claim 8 is applied to the method reclaiming hydrogenchloride, and it is characterized in that, described carrier is the mixture of magnesium oxide and hydroxy chloride magnesium, and wherein the molar content of hydroxy chloride magnesium should be no less than 10%.
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| CN201510121257.7A CN104744209B (en) | 2015-03-19 | 2015-03-19 | For moving-burden bed reactor and its application that ammonium chloride recycle chemistry chain reclaims ammonia and hydrogen chloride |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105836758A (en) * | 2016-06-15 | 2016-08-10 | 浙江大学 | Integral pyrolysis device and pyrolysis process for ammonium chloride based on cross flow heat exchange |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4305917A (en) * | 1979-10-06 | 1981-12-15 | Chemische Werke Huls Ag | Method for preparing ammonia and hydrogen chloride from ammonium chloride |
| CN202099245U (en) * | 2011-06-28 | 2012-01-04 | 西北化工研究院 | Pyrolysis reactor for powdered coal with low coal rank |
| CN103626206A (en) * | 2013-11-20 | 2014-03-12 | 浙江大学 | Sodium carbonate-vinyl chloride coproduction technique based on ammonium chloride chemical looping |
-
2015
- 2015-03-19 CN CN201510121257.7A patent/CN104744209B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4305917A (en) * | 1979-10-06 | 1981-12-15 | Chemische Werke Huls Ag | Method for preparing ammonia and hydrogen chloride from ammonium chloride |
| CN202099245U (en) * | 2011-06-28 | 2012-01-04 | 西北化工研究院 | Pyrolysis reactor for powdered coal with low coal rank |
| CN103626206A (en) * | 2013-11-20 | 2014-03-12 | 浙江大学 | Sodium carbonate-vinyl chloride coproduction technique based on ammonium chloride chemical looping |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105836758A (en) * | 2016-06-15 | 2016-08-10 | 浙江大学 | Integral pyrolysis device and pyrolysis process for ammonium chloride based on cross flow heat exchange |
| CN105836758B (en) * | 2016-06-15 | 2018-06-19 | 浙江大学 | A kind of monoblock type ammonium chloride pyrolysis installation and pyrolytic process based on cross-flow heat exchange |
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| CN104744209B (en) | 2017-03-15 |
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